CN111871159A - Membrane separation coupling alcohol amine solution for capturing flue gas CO2Apparatus and method - Google Patents
Membrane separation coupling alcohol amine solution for capturing flue gas CO2Apparatus and method Download PDFInfo
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- 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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- B01D53/34—Chemical or biological purification of waste gases
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- 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
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Abstract
The invention provides a method for trapping flue gas CO by coupling membrane separation with alcohol amine solution2The device comprises a membrane separator consisting of a single-stage membrane component, wherein a gas input port of the membrane separator is connected with a compressor, one output port of the membrane separator is a trapped gas outlet, the other gas output port of the membrane separator is a permeated gas outlet, one part of permeated gas enters a buffer tank, one part of permeated gas enters an absorption tower, the buffer tank is connected with the compressor, the compressor compresses the gas in the buffer tank, and CO obtained in the absorption tower2Discharged into CO2And the recovery device is used for feeding the rich liquid absorbed in the absorption tower into the regeneration tower. The invention also provides a method for trapping flue gas CO by coupling the membrane separation with the alcohol amine solution2Device for trapping flue gas CO2The method of (1). The invention provides a method for trapping flue gas by coupling membrane separation with alcohol amine solutionCO2The device and the method provide that the heat of high-temperature pressurized gas generated by compressing the flue gas by the compressor is transferred to the bottom of the regeneration tower through the heat pump before entering the membrane so as to heat the rich liquid to replace a boiler, thereby realizing the reduction of energy consumption and the utilization of heat and also finishing the aim of highly separating carbon dioxide.
Description
Technical Field
The invention belongs to the technical field of gas separation, and relates to a membrane separation and coupling alcohol amine solution for trapping flue gas CO2An apparatus and method.
Background
The method is characterized in that carbon dioxide discharged by industry and energy production is collected, and is a target which is pursued for a long time in a plurality of countries including China, and China announces in the action of strengthening coping with climate change, namely China independent contribution, that the independent action target of China is to reach the peak value of carbon dioxide discharge in 2030 years and strive to reach the peak value as early as possible. Therefore, carbon capture is of particular importance.
At present, carbon capture methods mainly comprise a chemical absorption method, a physical adsorption method, a membrane separation method and the like, the chemical absorption method is accepted by the market, carbon dioxide with the purity of 99.9% can be obtained by the chemical absorption method to meet the requirement of multipurpose use, but the pure chemical absorption method always has the problem of high energy consumption, particularly the problem of high regeneration energy consumption in the regeneration process of a chemical absorbent, a large amount of water vapor is needed for supplying heat to heat a solution to the regeneration temperature of 393K, and the energy consumption accounts for 50-80% of the total energy consumption of the whole CO2 capture process. Patent CN103566712A proposes that the waste gas at the top of the regeneration tower is used to drive a turbine to generate electricity to regenerate and supplement energy for the reboiler so as to reduce the regeneration energy consumption.
The membrane separation process of the carbon dioxide drives the carbon dioxide separation by utilizing the pressure difference on two sides of the membrane, the device for recovering the carbon dioxide by the membrane separation method is simple, convenient to operate and environment-friendly, does not need steam to provide heat, and is the most rapidly developed energy-saving method for recovering the carbon dioxide at present, but the purity of the carbon dioxide which can be realized by the multistage membrane component is about 95 percent, and the aim of capturing the high-purity carbon dioxide cannot be achieved. Patent CN107641535 proposes a device and method for separating and purifying various gases by membrane cryogenic coupling, in which carbon dioxide is purified by a first, a second and a third purification devices, and each purification device contains two or more membrane separators.
There are also patent reports that physical absorption and chemical absorption methods are used in combination to reduce the energy consumption for carbon dioxide regeneration and improve the separation degree of carbon dioxide, wherein CN105268283 proposes a combined absorption carbon dioxide capture process, which combines the traditional physical absorption and chemical absorption, adopts a high-pressure absorption-medium-pressure desorption strategy to reduce the capture energy consumption, and has a complex process flow and needs multi-stage compression and interstage cooling.
Disclosure of Invention
1. The technical problem to be solved is as follows:
the existing carbon capture is concentrated and has good effect, either the structure is complex or the regeneration energy consumption is high. The device for recovering the carbon dioxide by the membrane separation method is simple and convenient to operate, but the purity of the carbon dioxide obtained by single-stage and two-stage membrane separation is not high.
2. The technical scheme is as follows:
the invention aims to provide a method for treating flue gas CO2The scheme is suitable for the gas membrane separation process of the membrane component, and solves the problems that the regeneration energy consumption of the alcohol amine solution is high and the separation degree of the separated gas of the membrane component is not high in the existing low-concentration carbon dioxide. The invention provides a method for trapping flue gas CO by coupling membrane separation with alcohol amine solution2The device comprises a membrane separator, wherein a gas inlet of the membrane separator is connected with a compressor, the membrane separator is provided with two gas outlets, one outlet is a trapped gas outlet and is used for emptying outwards or conveying the trapped gas into raw material gas to be compressed by the compressor, the other gas outlet is a permeating gas outlet, one part of permeating gas enters a buffer tank, the other part of permeating gas enters an absorption tower, the buffer tank is connected with the compressor, the compressor compresses the gas in the buffer tank, and CO obtained in the absorption tower2Discharged into CO2And the recovery device is used for feeding the rich liquid absorbed in the absorption tower into the regeneration tower.
And a heat pump is arranged between the compressor and the bottom of the regeneration tower, and the heat of the gas compressed by the compressor 2 is transferred to the pregnant solution through the heat pump.
The gas in the buffer tank is compressed by a compressor, the temperature of the gas is raised to 48-95 ℃, and the pressure of the gas is 0.2-1.5 Mpa.
The temperature of the gas in the buffer tank is raised to 55-74 ℃ after the gas is compressed by the compressor, and the gas pressure is 0.4-0.8 Mpa.
And in the permeate gas outlet, 65-92% of permeate gas is merged into feed gas and enters the buffer tank, and 8-35% of permeate gas is connected with the gas inlet of the absorption tower, wherein the percentage is volume ratio.
The raw material gas is one or a mixture of a plurality of kinds of power plant flue gas, chemical plant flue gas and steel plant flue gas.
The membrane module is a single-stage membrane module.
The compression times of the compressor are single-stage or multi-stage compression.
The invention also provides the flue gas CO trapping by the membrane separation coupling alcohol amine solution2Device for trapping flue gas CO2The method of (1).
3. Has the advantages that:
the invention provides a method for trapping flue gas CO by coupling membrane separation with alcohol amine solution2The device and the method provide that the heat of high-temperature pressurized gas generated by compressing flue gas by a compressor is transferred to the bottom of a regeneration tower through a heat pump before the high-temperature pressurized gas enters a single-stage membrane module to heat rich liquid to replace a boiler, so that the energy consumption reduction and the heat utilization are realized, and the aim of highly separating carbon dioxide can be fulfilled.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Description of reference numerals: 1-a buffer tank 2-a compressor 3-a membrane module 4-a heat pump 5-an absorption tower 6-a regeneration tower.
Detailed Description
The present invention will be described in detail below with reference to the drawings and examples.
As shown in figure 1, a membrane separation coupling alcohol amine solution for capturing flue gas CO2Apparatus, including a membrane separator 3, characterized in that: the gas inlet of the membrane separator 3 is connected with the compressor 2, and the membrane separation is carried outThe device 3 has two gas output ports, and an export of gas is held back to output taste, and external evacuation or carry to the feed gas in by the compressor compression, another gas output port are the infiltration gas export, and one of them part infiltration gas enters into buffer tank 1, and a part infiltration gas enters into absorption tower 5, buffer tank 1 and compressor 2 are connected, compressor 2 compresses the gas in the buffer tank 1, the CO that obtains in the absorption tower 52Discharged into CO2And the recovery device is used for feeding the rich liquid absorbed in the absorption tower 5 into a regeneration tower 6.
The process takes the flue gas as the raw material gas, the gas compressed by the compressor 2 firstly passes through the heat pump 4 and then passes through the membrane component 3, one part of the permeated gas is mixed with the raw material gas and is continuously compressed, the other part of the permeated gas enters the absorption tower 5 and is absorbed by the alcohol amine solution, the high-temperature flue gas obtained by compressing the absorbed rich solution is heated to the regeneration temperature of 100-.
The invention also provides the flue gas CO trapping by the membrane separation coupling alcohol amine solution2Device for trapping flue gas CO2The method comprises the following steps: step S01: the raw material gas is compressed by the compressor 2 through the buffer tank 1, and the step S02: the gas compressed by the compressor 2 firstly passes through the heat pump 4 and then enters the membrane separator 3, the heat pump 4 heats the gas and transmits the heat to the rich liquid at the bottom of the regeneration tower 6 to heat and regenerate the rich liquid; step S03: one output flavor intercepted gas outlet of the membrane separator 3 is emptied outwards or conveyed into raw material gas to be compressed, the other gas output port is a permeating gas outlet, wherein one part of permeating gas enters the buffer tank 1, and one part of permeating gas enters the absorption tower 5; step S04: the gas is absorbed by alcohol amine solution in an absorption tower 5, the absorbed rich solution enters a regeneration tower 6, and CO obtained in the absorption tower 52Discharge of CO2And (5) a recovery device.
The temperature of the rich liquid delivered by the heat pump is 100-110 ℃ in step S02.
Example 1
The method of the embodiment has the following steps:
the device of the attached drawing is used for evaluating the carbon dioxide trapping performance, the raw material gas is compressed by a compressor and then enters a membrane separator, part of the permeation gas is merged into a raw material gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and the pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO212% of, O28% of N2It had a composition of 80%. The pressure of the compressed and heat-exchanged gas in the compressor 1 is 0.3MPa, the temperature is 45 ℃, and CO in the permeating gas is2The content is 32.4%, the gas entering the chemical absorption tower 5 accounts for 15% of the permeation gas, and the carbon dioxide concentration of the product gas is 93.2%.
Example 2
The method of the embodiment has the following steps:
a carbon dioxide capture performance evaluation test is carried out by using a device shown in the attached drawing, raw gas is compressed by a compressor 2 and then enters a membrane separator 3, part of permeation gas is merged into a raw gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and a pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO212% of, O28% of N2It had a composition of 80%. The pressure of the gas after the compressor is subjected to three-stage compression and heat exchange is 0.5MPa, the temperature is 47 ℃, and CO in the permeating gas2The content is 42%, the gas entering the chemical absorption tower accounts for 15% of the permeating gas, and the carbon dioxide concentration of the product gas is 94.6%.
Example 3
The method of the embodiment has the following steps:
a carbon dioxide capture performance evaluation test is carried out by using a device shown in the attached drawing, raw gas is compressed by a compressor 2 and then enters a membrane separator 3, part of permeation gas is merged into a raw gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and a pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO2Is 12 percent of the total weight of the mixture,O28% of N2It had a composition of 80%. The pressure of the gas after the compressor is subjected to secondary compression and heat exchange is 0.68MPa, the temperature is 52 ℃, and CO in the permeating gas is2The content is 46%, the gas entering the chemical absorption tower accounts for 16% of the permeating gas, and the carbon dioxide concentration of the product gas is 95.9%.
Example 4
The method of the embodiment has the following steps:
a carbon dioxide capture performance evaluation test is carried out by using a device shown in the attached drawing, raw gas is compressed by a compressor 2 and then enters a membrane separator 3, part of permeation gas is merged into a raw gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and a pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO212% of, O28% of N2It had a composition of 80%. The pressure of the compressed and heat-exchanged gas in the compressor is 0.5MPa, the temperature is 46 ℃, and CO in the permeating gas2The content is 42%, the gas entering the chemical absorption tower accounts for 20% of the permeation gas, and the carbon dioxide concentration of the product gas is 93.1%.
Example 5
The method of the embodiment has the following steps:
a carbon dioxide capture performance evaluation test is carried out by using a device shown in the attached drawing, raw gas is compressed by a compressor 2 and then enters a membrane separator 3, part of permeation gas is merged into a raw gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and a pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO215% of O25% of N2It had a composition of 80%. The pressure of the compressed and heat-exchanged gas in the compressor is 0.7MPa, the temperature is 48 ℃, and CO in the permeating gas2The content is 48%, the gas entering the chemical absorption tower accounts for 20% of the permeating gas, and the carbon dioxide concentration of the product gas is 96.2%.
Example 6
The method of the embodiment has the following steps:
a carbon dioxide capture performance evaluation test is carried out by using a device shown in the attached drawing, raw gas is compressed by a compressor 2 and then enters a membrane separator 3, part of permeation gas is merged into a raw gas buffer tank 1, the other part of the permeation gas enters a chemical absorption tower 5, and a pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO212% of, O28% of N2It had a composition of 80%. The pressure of the compressed and heat-exchanged gas in the compressor is 0.8MPa, the temperature is 49 ℃, and CO in the permeating gas2The content is 48%, the gas entering the chemical absorption tower accounts for 15% of the permeating gas, and the carbon dioxide concentration of the product gas is 99.9%.
Example 7
The method of the embodiment has the following steps:
the device of the attached drawing is used for carrying out a carbon dioxide capture performance evaluation test, raw gas enters a membrane separator after being compressed by a compressor, part of permeation gas is merged into a raw gas buffer tank, the other part of the permeation gas enters a chemical absorption tower, and the pregnant solution after chemical absorption is regenerated.
The raw material gas is simulated flue gas, the temperature is 40 ℃, the pressure is normal, and the raw material gas is prepared from CO212% of, O28% of N2It had a composition of 80%. The pressure of the gas after the compressor is subjected to secondary compression and heat exchange is 1.2MPa, the temperature is 50 ℃, and CO in the permeating gas is2The content is 48%, the gas entering the chemical absorption tower accounts for 18% of the permeating gas, and the carbon dioxide concentration of the product gas is 99.9%.
The percentages in the above 7 examples are volume percentages.
It can be seen from the above 7 examples that the carbon dioxide concentration of the product gas is at least 93.1%, and 99.9% is achieved in examples 6 and 7.
Claims (10)
1. Membrane separation coupling alcohol amine solution for capturing flue gas CO2Apparatus comprising a membrane separator (3), characterized in that: the gas input port of the membrane separator (3) is connected with the compressor (2), the membrane separator (3) is provided with two gas output ports, one gas output port for outputting flavor intercepting gas is emptied outwards or conveyed into raw material gas to be compressed by the compressorCompressing, wherein another gas outlet is a permeate gas outlet, one part of permeate gas enters the buffer tank (1), one part of permeate gas enters the absorption tower (5), the buffer tank (1) is connected with the compressor (2), the compressor (2) compresses the gas in the buffer tank (1), and the obtained CO in the absorption tower (5)2Discharged into CO2And the recovery device is used for feeding the rich liquid absorbed in the absorption tower (5) into a regeneration tower (6).
2. The membrane separation coupling alcohol amine solution for capturing flue gas CO according to claim 12The device is characterized in that: a heat pump (4) is arranged between the compressor (2) and the bottom of the regeneration tower (6), and heat of gas compressed by the compressor (2) is transferred to the rich liquid through the heat pump (4).
3. The membrane separation coupling alcohol amine solution for capturing flue gas CO according to claim 12The device is characterized in that: the gas in the buffer tank (1) is compressed by the compressor (2), the gas temperature is raised to 48-95 ℃, and the gas pressure is 0.2-1.5 Mpa.
4. The membrane separation coupling alcohol amine solution for capturing flue gas CO according to claim 32The device is characterized in that: the gas in the buffer tank (1) is compressed by the compressor (2), the gas temperature is raised to 55-74 ℃, and the gas pressure is 0.4-0.8 Mpa.
5. The membrane separation coupling alcohol amine solution as claimed in any one of claims 1 to 4 for capturing flue gas CO2The device is characterized in that: and in the permeate gas outlet, 55-90% of permeate gas is merged into feed gas and enters the buffer tank (1), and 10-45V% of permeate gas is connected with the gas inlet of the absorption tower (5), wherein the percentage is volume ratio.
6. The membrane separation coupling alcohol amine solution for capturing flue gas CO according to claim 52The device is characterized in that: the raw material gas is the flue gas of a power plant,One or more of flue gas of a chemical plant and flue gas of an iron and steel plant.
7. The membrane separation coupling alcohol amine solution as claimed in any one of claims 1 to 4 and 6 for capturing flue gas CO2The device is characterized in that: the membrane separator (3) is a single-stage membrane component.
8. The membrane separation coupling alcohol amine solution as claimed in any one of claims 1 to 4 and 6 for capturing flue gas CO2The device is characterized in that: the compression frequency of the compressor (2) is single-stage or multi-stage compression.
9. Use of the membrane separation coupling alcohol amine solution of any one of claims 1 to 8 for capturing flue gas CO2Device for trapping flue gas CO2The method comprises the following steps: step S01: the raw material gas is compressed by a compressor (2) through a buffer tank (1), and the step S02: the gas compressed by the compressor (2) firstly passes through the heat pump (4) and then enters the membrane separator (3), the heat pump (4) heats the gas and transmits the heat to the rich liquid at the bottom of the regeneration tower (6) to heat and regenerate the rich liquid; step S03: one output flavor intercepted gas outlet of the membrane separator (3) is emptied outwards or is conveyed into raw material gas to be compressed, the other gas outlet is a permeating gas outlet, wherein one part of permeating gas enters the buffer tank (1), and one part of permeating gas enters the absorption tower (5); step S04: the gas is absorbed by alcohol amine solution in an absorption tower (5), the absorbed rich solution enters a regeneration tower (6), and CO obtained in the absorption tower (5)2Discharged into CO2And (5) a recovery device.
10. The method of claim 9, wherein; the temperature of the rich liquid delivered by the heat pump is 100-110 ℃ in step S02.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112516758A (en) * | 2020-12-13 | 2021-03-19 | 天津大学 | Secondary membrane separation system and method for capturing carbon dioxide in flue gas |
| CN114011212A (en) * | 2021-10-30 | 2022-02-08 | 雅邦绿色过程与新材料研究院南京有限公司 | An energy-saving process for the coupled recovery of high-concentration CO2 by membrane/MDEA solution |
| CN114159954A (en) * | 2021-12-07 | 2022-03-11 | 兰州理工大学 | Phase change solvent coupling membrane separation flue gas CO2System and method |
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