CN117839396A - Low-temperature phase change based coupling carbon trapping process - Google Patents
Low-temperature phase change based coupling carbon trapping process Download PDFInfo
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- CN117839396A CN117839396A CN202410096652.3A CN202410096652A CN117839396A CN 117839396 A CN117839396 A CN 117839396A CN 202410096652 A CN202410096652 A CN 202410096652A CN 117839396 A CN117839396 A CN 117839396A
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- 238000000034 method Methods 0.000 title claims abstract description 47
- 230000008569 process Effects 0.000 title claims abstract description 38
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 29
- 230000008878 coupling Effects 0.000 title claims abstract description 11
- 238000010168 coupling process Methods 0.000 title claims abstract description 11
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 11
- 230000008859 change Effects 0.000 title description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 132
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 66
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 66
- 239000007789 gas Substances 0.000 claims abstract description 55
- 238000004581 coalescence Methods 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 43
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003546 flue gas Substances 0.000 claims abstract description 35
- 239000012528 membrane Substances 0.000 claims abstract description 32
- 230000007704 transition Effects 0.000 claims abstract description 15
- 239000012530 fluid Substances 0.000 claims abstract description 11
- 239000002912 waste gas Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims description 61
- 239000012071 phase Substances 0.000 claims description 42
- 238000001816 cooling Methods 0.000 claims description 13
- 239000007791 liquid phase Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 5
- 239000012466 permeate Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000012465 retentate Substances 0.000 claims description 2
- 230000000087 stabilizing effect Effects 0.000 claims description 2
- 238000002485 combustion reaction Methods 0.000 abstract description 6
- 229910000831 Steel Inorganic materials 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 5
- 239000010959 steel Substances 0.000 abstract description 5
- 238000010521 absorption reaction Methods 0.000 abstract description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 abstract description 4
- 239000001301 oxygen Substances 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000003139 buffering effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 238000001926 trapping method Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000005371 permeation separation Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Aiming at the problems of difficult separation of high-concentration and high-impurity carbon dioxide flue gas generated by oxygen-enriched combustion in the steel industry, chemical absorption methods of coal-fired power plants and the like, a coupling carbon trapping process based on low-temperature phase transition is provided, a main process route adopts a two-stage low-temperature phase transition trapping process, the coupling cyclone separation, coalescence separation and membrane separation processes are integrated in the two-stage low-temperature phase transition trapping process, and the coupling membrane separation process purifies carbon dioxide in the generated waste gas, so that the concentration of carbon dioxide in fluid entering a second-stage cyclone separator is higher, the influence of impurity gas on the low-temperature separation of the second-stage cyclone separator is reduced, the application range of the carbon trapping process is improved, and finally the process has the advantages of higher trapping rate, higher purity of the trapped carbon dioxide and the like.
Description
Technical Field
The invention belongs to the technical field of carbon trapping processes, and particularly relates to a coupling carbon trapping process based on low-temperature phase transition, which is particularly suitable for trapping carbon in flue gas with high carbon dioxide concentration.
Background
In recent years, energy and environmental issues have attracted worldwide attention, and there is an urgent need to use reasonable, sustainable fossil fuels with less environmental impact. As one of the most important greenhouse gases, CO produced by the combustion of fossil fuels 2 Play an important role in climate change. Among the various emissions sources, coal-fired power plants are the most prominent CO worldwide 2 One of the emissions sources, emits about 20 million tons of CO per year 2 . Global CO in the past few decades 2 Emissions increased rapidly, according to the inter-government climate change committee report, by 2100 years, CO in the atmosphere 2 Levels as high as 570ppm are possible, resulting in an average global air temperature rise of about 1.9 ℃ and an average sea level rise of 3.8 meters.
Carbon dioxide capture, utilization and sequestration (CCUS) is a promising strategy by capturing CO from large point sources such as coal-fired power plants, the steel and cement industries, and the like 2 Sealing it in porous rock or reusing it in oil extraction, fertilizer and chemical synthesis, etc. to reduce CO 2 Is arranged in the air. CO can be captured and stored by adding a carbon dioxide capturing and storing device in a traditional power plant 2 The discharge amount is reduced by about 80-90%.
Membrane separation process utilizing CO 2 The difference of partial pressure and concentration of the gas on both sides of the membrane is used as driving force to make CO 2 The molecules rapidly pass through the separation membrane and are enriched on the other side of the membrane, and the membrane separation method is used for CO 2 Is separated from CO by membrane material 2 Is determined by the permeability and selectivity of the catalyst. Compared with other trapping methods after combustion, the membrane separation method has the advantages of low investment cost, environmental friendliness, low energy consumption, easy miniaturization, skid-mounted property and the like, but the use condition of the membrane separation method is relatively harsh.
Cryogenic phase-change carbon dioxide capture technology, commonly referred to as cryogenic carbon capture, relies on phase change to separate carbon dioxide from gas in liquid or solid form, low temperature capture of CO compared to other capture methods 2 The purity of the product is high, but the low-temperature trapping requires a compressor to compress the mixed gas of the flowing gas to a high-pressure low-temperature state, the energy consumption is relatively large, and the CO 2 Separation is difficult with low purity.
In addition, for large amounts of CO captured 2 The product is a typical treatment link which is difficult to avoid, and the storage place is far away from CO 2 The trapping device, the liquid carbon dioxide product is often easier to transport over long distances.
Disclosure of Invention
In combination with the technical situation, the invention provides a coupling carbon trapping process based on low-temperature phase transition aiming at the problems of difficult separation of high-concentration and high-impurity carbon dioxide smoke generated by oxygen-enriched combustion in the steel industry, chemical absorption method of coal-fired power plants and the like, wherein a main process route adopts a two-stage low-temperature phase transition trapping process, and the coupling cyclone separation, coalescence separation and membrane separation processes are integrated in the two-stage low-temperature phase transition trapping process, so that the coupling membrane separation process is used for purifying carbon dioxide in the generated waste gas, the concentration of carbon dioxide in fluid entering a second-stage cyclone separator is higher, the influence of impurity gas on the low-temperature separation of the second-stage cyclone separator is reduced, the application range of the carbon trapping process is improved, and finally, the process has higher trapping rate and the purity of the trapped carbon dioxide is higher.
The technical scheme adopted by the invention is as follows: a low-temperature phase change-based coupled carbon capture process comprises a first compressor, a first heat exchanger, a first cyclone separator, a first coalescence separator, a second heat exchanger, a membrane separator, a second compressor, a third heat exchanger, a second cyclone separator and a second coalescence separator.
The inlet of the primary compressor is connected with a flue gas incoming flow pipeline, the outlet of the primary compressor is communicated with the inlet of the primary cyclone separator after passing through the first heat exchanger, the light phase overflow port of the primary cyclone separator is connected with the primary coalescence separator, and the underflow port of the primary cyclone separator and the liquid phase outlet of the primary coalescence separator are both communicated with a liquid carbon dioxide collecting tank; the gas phase outlet of the primary coalescence separator is connected with the inlet of the membrane separator after passing through the second heat exchanger, the permeate gas outlet pipe of the membrane separator is communicated with the inlet of the secondary compressor, the outlet of the secondary compressor is communicated with the inlet of the secondary cyclone separator after passing through the third heat exchanger, the light phase overflow port of the secondary cyclone separator is connected with the secondary coalescence separator, and the underflow port of the secondary cyclone separator and the liquid phase outlet of the secondary coalescence separator are both communicated with a liquid carbon dioxide collecting tank; the gas phase outlet of the membrane separator and the gas phase outlet of the secondary coalescing separator are externally connected to an exhaust gas treatment device.
Further, the system further comprises a primary buffer tank and a secondary buffer tank, wherein the primary buffer tank is connected between the primary compressor and the first heat exchanger, and the secondary buffer tank is connected between the secondary compressor and the third heat exchanger.
Further, the self-circulation heat exchange system comprises two cooling modules and a circulation pipeline, wherein the two cooling modules are respectively used for cooling the primary compressor and the secondary compressor, and a medium in the circulation pipeline absorbs heat generated by the working of the two compressors and flows through the second heat exchanger to supply the heat.
The liquid carbon dioxide collecting tank can adopt one tank or a plurality of tanks to facilitate the space matching of equipment, for example, the liquid carbon dioxide collecting tank comprises a first liquid carbon dioxide collecting tank and a second liquid carbon dioxide collecting tank; the underflow opening of the first-stage cyclone separator and the liquid phase outlet of the first-stage coalescence separator are communicated to a first liquid carbon dioxide collecting tank, and the underflow opening of the second-stage cyclone separator and the liquid phase outlet of the second-stage coalescence separator are communicated to a second liquid carbon dioxide collecting tank.
Further, the exhaust gas treatment device employs an exhaust gas collection tank. The first heat exchanger, the second heat exchanger and the third heat exchanger are all shell-and-tube heat exchangers.
The invention also claims a coupling carbon trapping method based on low-temperature phase transition, which adopts the carbon trapping process as described above, and specifically comprises the following steps:
(1) After the device is started, the flue gas containing high-concentration carbon dioxide enters the device in the process; after the inflow of the flue gas is stabilized, starting a first-stage compressor to boost the pressure to a set pressure, enabling high-pressure flue gas generated by the first-stage compressor to enter a first-stage heat exchanger for cooling and liquefying, enabling gas-liquid mixture flue gas to enter a first-stage cyclone separator for gas-liquid separation when the temperature is reduced to the set temperature, collecting separated liquid carbon dioxide, enabling light-phase overflow fluid of the first-stage cyclone separator to enter a first-stage coalescence separator for gas-liquid re-separation, and opening a valve in a pipeline when the bottom outlet pressure of the first-stage coalescence separator reaches the set value, and collecting the separated liquid carbon dioxide at the bottom of the first-stage coalescence separator;
(2) When the pressure of the top outlet of the primary coalescence-separator reaches a set value, opening an inlet valve of a second heat exchanger, heating the gas phase in the second heat exchanger, opening the inlet valve of the membrane separator to separate the gas after the gas phase reaches the temperature required by the membrane separator, pressurizing the permeate gas in a secondary compressor, and enabling the retentate gas to enter waste gas treatment equipment;
(3) Pressurizing the permeation gas to a set pressure through a secondary compressor, enabling high-pressure flue gas to enter a third heat exchanger for cooling and liquefying, enabling gas-liquid mixed flue gas to enter a secondary cyclone separator for gas-liquid separation when the temperature is reduced to the set temperature, collecting liquid carbon dioxide separated from the bottom of the secondary cyclone separator, enabling light-phase overflow fluid of the secondary cyclone separator to enter a secondary coalescence separator for gas-liquid re-separation, opening a valve in a pipeline when the outlet pressure of the bottom of the secondary coalescence separator reaches the set value, collecting liquid carbon dioxide separated from the bottom of the secondary coalescence separator, and enabling gas phase separated from the top of the secondary coalescence separator to enter waste gas treatment equipment; the final product carbon dioxide is stored in the liquid carbon dioxide collecting tank, so that the transportation is convenient, and the advantage of high-efficiency high-purity carbon dioxide trapping can be achieved.
Further, in the process of the steps of the method, before the high-pressure flue gas generated by the primary compressor enters the first heat exchanger, the pressure and the flow are stabilized in the primary buffer tank; and before the high-pressure flue gas generated by the secondary compressor enters the third heat exchanger, stabilizing the pressure and flow in the secondary buffer tank.
The technical scheme of the invention has the advantages that:
1. the coalescing treatment and the membrane separation are coupled between the two-stage cyclone separation and trapping processes, so that the concentration of carbon dioxide in the mixed fluid entering the second-stage cyclone separator is greatly improved, the carbon trapping process can meet the process requirements of difficult separation caused by low purity of carbon dioxide in flue gas generated by oxygen-enriched combustion in the steel industry, chemical absorption methods of coal-fired power plants and the like, and the high-efficiency carbon trapping effect is obtained.
2. The heat energy generated by the operation of the secondary compressor is used for fluid parameter treatment before the membrane separation process, so that the heat energy waste is avoided, and the energy utilization efficiency is improved.
Drawings
FIG. 1 is a flow chart of a coupled carbon capture process based on low temperature phase change of the present invention;
in the figure: f1 to F12 represent flue gas or flue gas of gas-liquid mixture; p1 to P4 represent liquid carbon dioxide streams; Q1-Q2 represent exhaust gas streams;
1. the device comprises a first-stage compressor, 2, a first-stage buffer tank, 3, a first heat exchanger, 4, a first-stage cyclone separator, 5, a first-stage coalescence separator, 6, a first liquid carbon dioxide collecting tank, 7, a second heat exchanger, 8, a membrane separator, 9, a second-stage compressor, 10, an exhaust gas collecting tank, 11, a second-stage buffer tank, 12, a third heat exchanger, 13, a second-stage cyclone separator, 14, a second-stage coalescence separator, 15 and a second liquid carbon dioxide collecting tank.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative only and are not to be construed as limiting the invention.
In the description of the present invention, it should be understood that the terms "center," "upper," "lower," "front," "rear," "left," "right," "inner," "outer," and the like indicate orientations or positional relationships that are used to simplify the description, and are not meant to indicate or imply that the devices or components being referred to must be in a particular orientation, be configured and operated in a particular orientation, and are not to be construed as limiting the invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be the communication between the two parts. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
Referring to fig. 1, the low-temperature phase-change-based coupled carbon trapping process flow chart of the invention comprises two stages of cyclone separation processes connected in series, pressurizing and cooling equipment is arranged in front of each stage of cyclone separation equipment, a gas enrichment membrane separation process is coupled between the two stages of cyclone separation processes, carbon trapping at high treatment speed of flue gas is ensured, and the problem of difficult separation caused by low purity of carbon dioxide in the flue gas is solved.
As shown in the figure, the system comprises a first-stage compressor 1, a first-stage buffer tank 2, a first heat exchanger 3, a first-stage cyclone separator 4, a first-stage coalescence separator 5, a second heat exchanger 7, a membrane separator 8, a second-stage compressor 9, a second-stage buffer tank 11, a third heat exchanger 12, a second-stage cyclone separator 13 and a second-stage coalescence separator 14, wherein flue gas flows into an inlet of the first-stage compressor 1, an outlet of the first-stage compressor 1 is communicated with the first-stage buffer tank 2 through a pipeline, the first-stage buffer tank 2 is communicated with the first-stage cyclone separator 4 after passing through the first heat exchanger 3, the first heat exchanger 3 can adopt a refrigerant medium to exchange heat with compressed flue gas in a countercurrent mode, carbon dioxide gas in high-pressure flue gas is cooled and liquefied, a cooled down gas mixture fluid is communicated with an inlet of the first-stage cyclone separator 4 after being cooled, a bottom flow port of the first-stage cyclone separator 4 is communicated with the first-liquid carbon dioxide collector through a pipeline, a light phase overflow port of the first-stage cyclone separator 4 is communicated with the coalescence separator 5, a liquid-state outlet of the coalescence separator 5 is communicated with the first-liquid carbon dioxide collector 6 through a pipeline, a liquid-state outlet of the first-stage cyclone separator 5 is communicated with the second-stage coalescence separator 7 through the second-stage coalescence separator 8 through the second-stage buffer tank 9, a gas inlet of the second-stage coalescence separator 9 is communicated with the second-stage coalescence separator 9 after passing through the second-stage gas separator 8 and the second-stage coalescence separator 2 is communicated with the second-stage gas separator 12 through the second-stage separator 12, the second-stage coalescence separator 2 is communicated with the inlet 12 through the inlet 12 after passing through the second-stage heat-stage separator 12, the inlet 12 is communicated with the second-stage separator 12, the gas separator pipeline is communicated with the gas separator pipeline through the inlet pipeline and the separator 3, the light phase overflow port of the secondary cyclone separator 13 is communicated with the secondary coalescing separator 14 through a pipeline, the liquid outlet pipe of the secondary coalescing separator 14 is communicated with the second liquid carbon dioxide collecting tank 15, and the gaseous outlet pipe of the secondary coalescing separator 14 is communicated with the waste gas collecting tank 10.
For ease of illustration, two tanks are provided, a first liquid carbon dioxide tank 6 and a second liquid carbon dioxide tank 15, it being apparent that only one liquid carbon dioxide tank may be used.
The carbon capturing process can be further coupled with a self-circulation heat exchange system, the self-circulation heat exchange system comprises two cooling modules and a circulation pipeline, the two cooling modules respectively cool down and cool down the primary compressor 1 and the secondary compressor 9, and medium in the circulation pipeline absorbs heat generated by the operation of the compressors, then flows through the second heat exchanger 7 to heat up mixed fluid from the primary coalescence-separation device 5, so that the working performance of the subsequent membrane separator 8 is guaranteed. The first heat exchanger 3, the second heat exchanger 7 and the third heat exchanger 12 can all adopt shell-and-tube heat exchangers.
In connection with the fluid flow path of the marking in fig. 1, the process based on the carbon capture process of the present invention is described as follows:
the method comprises the steps that oxygen-enriched combustion in the steel industry, a chemical absorption method of a coal-fired power plant and the like generate high-concentration carbon dioxide-containing flue gas F1, the flue gas F1 enters a carbon capture device, the pressure is increased to a specific pressure through a primary compressor 1, high-pressure flue gas F2 generated by the primary compressor 1 enters a primary buffer tank 2 for buffering, high-pressure gas F3 with stable pressure and flow rate enters a first heat exchanger 3 for cooling and liquefying, gas-liquid mixture flue gas F4 enters a primary cyclone separator 4 for gas-liquid separation, liquid phase P1 separated from the bottom enters a first liquid carbon dioxide collecting tank 6, separated gas phase F5 enters a primary coalescence separator 5 from an overflow port at the top for gas-liquid re-separation, and liquid phase P2 separated from the bottom of the primary coalescence separator 5 enters the first liquid carbon dioxide collecting tank 6; the gas phase F6 separated from the top of the primary coalescence-separation device 5 enters the second heat exchanger 7 for heating, after reaching the required optimal temperature of the membrane separator 8, the gas phase F6 enters the membrane separator 8 for permeation separation of carbon dioxide gas, permeation gas F8 enters the secondary compressor 9 for pressurization, trapped gas Q1 enters the waste gas collection tank 10, permeation gas F8 is pressurized to a specific pressure by the secondary compressor 9, high-pressure flue gas F9 enters the secondary buffer tank 11 for buffering, pressure and flow-stable high-pressure flue gas F10 enters the second heat exchanger 12 for cooling and liquefying, gas-liquid mixed flue gas F11 enters the secondary cyclone 13 for gas-liquid separation, liquid phase P3 separated from the bottom enters the second liquid carbon dioxide collection tank 15, gas phase F12 separated from the top overflow pipe enters the secondary coalescence-separation device 14 for gas-liquid re-separation, liquid phase P4 separated from the bottom of the secondary coalescence-separation device 14 enters the second liquid carbon dioxide collection tank 15, and waste gas Q2 separated from the top of the secondary coalescence-separation device is also discharged into the waste gas collection tank 10. The final product carbon dioxide is composed of carbon dioxide in the first liquid carbon dioxide collecting tank 6 and the second liquid carbon dioxide collecting tank 15, so that the advantage of high-efficiency and high-purity carbon dioxide capturing can be achieved. In the process, heat E1 generated by pressurization of the primary compressor 1 is transferred to the second heat exchanger 7, and heat E2 generated by pressurization of the secondary compressor 9 is also supplied to the second heat exchanger 7.
While the foregoing description of the embodiments of the present invention has been presented in conjunction with the drawings, it should be understood that it is not intended to limit the scope of the invention, but rather, it is intended to cover modifications or variations of the equivalent structures or equivalent processes, which may be accomplished by those skilled in the art without undue effort based on the teachings herein, or by direct or indirect application to other related arts, while remaining within the scope of the present invention.
Claims (8)
1. The coupling carbon capturing process based on low-temperature phase transition is characterized by comprising a first-stage compressor (1), a first heat exchanger (3), a first-stage cyclone separator (4), a first-stage coalescence separator (5), a second heat exchanger (7), a membrane separator (8), a second-stage compressor (9), a third heat exchanger (12), a second-stage cyclone separator (13) and a second-stage coalescence separator (14);
the inlet of the primary compressor (1) is connected with a flue gas incoming flow pipeline, the outlet of the primary compressor (1) is communicated with the inlet of the primary cyclone separator (4) after passing through the first heat exchanger (3), the light phase overflow port of the primary cyclone separator (4) is connected with the primary coalescence separator (5), and the underflow port of the primary cyclone separator (4) and the liquid phase outlet of the primary coalescence separator (5) are both communicated with a liquid carbon dioxide collecting tank;
the gas phase outlet of the primary coalescence separator (5) is connected with the inlet of the membrane separator (8) after passing through the second heat exchanger (7), the permeate gas outlet pipe of the membrane separator (8) is communicated with the inlet of the secondary compressor (9), the outlet of the secondary compressor (9) is communicated with the inlet of the secondary cyclone separator (13) after passing through the third heat exchanger (12), the light phase overflow port of the secondary cyclone separator (13) is connected with the secondary coalescence separator (14), and the bottom flow port of the secondary cyclone separator (13) and the liquid phase outlet of the secondary coalescence separator (14) are both communicated with the liquid carbon dioxide collecting tank;
the gas phase outlet of the membrane separator (8) and the gas phase outlet of the secondary coalescing separator (14) are externally connected to an exhaust gas treatment device.
2. The coupled carbon capture process based on low temperature phase transition of claim 1, further characterized by comprising a primary buffer tank (2) and a secondary buffer tank (11), the primary buffer tank (2) being connected between the primary compressor (1) and the first heat exchanger (3), the secondary buffer tank (11) being connected between the secondary compressor (9) and the third heat exchanger (12).
3. The low temperature phase transition based coupled carbon capture process of claim 1 or 2, further characterized by the liquid carbon dioxide collection tank comprising a first liquid carbon dioxide collection tank (6) and a second liquid carbon dioxide collection tank (15); the underflow opening of the primary cyclone separator (4) and the liquid phase outlet of the primary coalescing separator (5) are communicated to a first liquid carbon dioxide collecting tank (6), and the underflow opening of the secondary cyclone separator (13) and the liquid phase outlet of the secondary coalescing separator (14) are communicated to a second liquid carbon dioxide collecting tank (15).
4. The low temperature phase transition based coupled carbon capture process of claim 1 or 2, further characterized in that the exhaust gas treatment device employs an exhaust gas collection tank (10).
5. The coupled carbon capture process based on low temperature phase transition according to claim 1 or 2, further characterized by a self-circulation heat exchange system comprising two cooling modules, a primary compressor (1) and a secondary compressor (9) for cooling down respectively, and a circulation line in which a medium absorbs heat generated by the operation of the two compressors and flows through the second heat exchanger (7) to supply heat.
6. The low temperature phase transition based coupled carbon capture process of claim 1, further characterized in that the first heat exchanger (3), the second heat exchanger (7) and the third heat exchanger (12) are shell and tube heat exchangers.
7. A low-temperature phase transition based coupled carbon capturing method, which adopts the carbon capturing process as defined in any one of claims 1 to 6, and comprises the following steps:
(1) After the device is started, the flue gas containing high-concentration carbon dioxide enters the device in the process; after the inflow of the flue gas is stabilized, a first-stage compressor (1) is started to boost to a set pressure, high-pressure flue gas generated by the first-stage compressor (1) enters a first-stage heat exchanger (3) to be cooled and liquefied, when the temperature is reduced to the set temperature, gas-liquid mixture flue gas enters a first-stage cyclone separator (4) to be separated into gas and liquid, the separated liquid carbon dioxide is collected, light-phase overflow fluid of the first-stage cyclone separator (4) enters a first-stage coalescence separator (5) to be separated into gas and liquid again, and when the outlet pressure at the bottom of the first-stage coalescence separator (5) reaches the set value, a valve in a pipeline is opened to collect the liquid carbon dioxide separated from the bottom of the first-stage coalescence separator (5);
(2) When the outlet pressure at the top of the first-stage coalescence-separation device (5) reaches a set value, opening an inlet valve of a second heat exchanger (7), heating the gas phase in the second heat exchanger (7), opening an inlet valve of the membrane separator (8) to separate gas after the gas phase reaches the temperature required by the membrane separator (8), pressurizing the permeate gas in a second-stage compressor (9), and introducing the retentate gas into waste gas treatment equipment;
(3) The permeation gas is pressurized to a set pressure through a secondary compressor (9), high-pressure flue gas enters a third heat exchanger (12) for cooling and liquefying, when the temperature is reduced to the set temperature, gas-liquid mixed flue gas enters a secondary cyclone separator (13) for gas-liquid separation, liquid carbon dioxide separated from the bottom of the secondary cyclone separator (13) is collected, light-phase overflow fluid of the secondary cyclone separator (13) enters a secondary coalescence separator (14) for gas-liquid re-separation, when the outlet pressure of the bottom of the secondary coalescence separator (13) reaches the set value, a valve in a pipeline is opened, liquid carbon dioxide separated from the bottom of the secondary coalescence separator (14) is collected, and gas phase separated from the top of the secondary coalescence separator (14) enters waste gas treatment equipment.
8. The method according to claim 7, further characterized by stabilizing the pressure and flow in the primary buffer tank (2) before the high pressure flue gas generated by the primary compressor (1) enters the first heat exchanger (3); before the high-pressure flue gas generated by the secondary compressor (9) enters the third heat exchanger (12), the pressure and the flow are stabilized in the secondary buffer tank (11).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202410096652.3A CN117839396A (en) | 2024-01-23 | 2024-01-23 | Low-temperature phase change based coupling carbon trapping process |
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| CN202410096652.3A CN117839396A (en) | 2024-01-23 | 2024-01-23 | Low-temperature phase change based coupling carbon trapping process |
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| CN117839396A true CN117839396A (en) | 2024-04-09 |
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