CN116196726A - Carbon dioxide trapping system for mineralized aerated block production - Google Patents

Carbon dioxide trapping system for mineralized aerated block production Download PDF

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Publication number
CN116196726A
CN116196726A CN202310108272.2A CN202310108272A CN116196726A CN 116196726 A CN116196726 A CN 116196726A CN 202310108272 A CN202310108272 A CN 202310108272A CN 116196726 A CN116196726 A CN 116196726A
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tower
regeneration
carbon dioxide
solution
lean
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彭兵
周维英
张奔
张亨玮
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Anhui Chuanyin Technology Information Service Co ltd
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Anhui Chuanyin Technology Information Service Co ltd
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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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
    • 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
    • B01D53/002—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 condensation
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • 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
    • B01D53/14—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 absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • B01D53/14—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 absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • 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

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a carbon dioxide trapping system for mineralized aerated block production, and relates to the technical field of mineralized aerated block production. The system comprises a fan, a washing liquid storage tank, an absorption tower and a regeneration tower, wherein the outlet at the lower end of the absorption tower is communicated with the first inlet of a lean-rich liquid heat exchanger through a rich liquid pump, the first outlet of the lean-rich liquid heat exchanger is communicated with the inlet at the upper end of the regeneration tower, the outlet at the lower end of the regeneration tower is communicated with the second inlet of the lean-rich liquid heat exchanger, and the second outlet of the lean-rich liquid heat exchanger is communicated with the inlet at the upper end of the absorption tower through a lean liquid pump and a lean liquid cooler. In the system, the composite amine solution based on monoethanolamine is adopted, and the antioxidant and the corrosion inhibitor are used as carbon dioxide absorbent, so that the high absorption rate, high absorption load and low regeneration energy consumption of the carbon dioxide absorbent are utilized, the high absorption capacity of the solution to CO2 is maintained, the regeneration energy consumption of the solution is reduced, and the equipment corrosion is reduced.

Description

Carbon dioxide trapping system for mineralized aerated block production
Technical Field
The invention belongs to the technical field of mineralized aerated block production, and particularly relates to a carbon dioxide trapping system for mineralized aerated block production.
Background
The mineralized aerated block is a building block produced by taking industrial wastes such as fly ash, tailing sand, desulfurized gypsum and the like as raw materials, and generates a lot of harmful gas mixed with smoke dust in the production and manufacturing process of the mineralized aerated block, wherein carbon dioxide is one of main pollution gases, is one of main components of greenhouse gases which cause global climate warming, and how to capture and reuse discharged carbon dioxide is an important research direction in the field of current flue gas purification.
In the conventional art, carbon dioxide is generally captured by using an amine liquid as an absorbent, and a carbon capturing system formed by the carbon capturing system mainly comprises an absorption tower, a desorption tower, a reboiler and the like. However, the system has a problem;
1. because the amine liquid used by the existing carbon dioxide trapping system is used as an absorbent to trap carbon dioxide, the regenerability and corrosion resistance are low, so that the energy consumption of the whole system is serious, and the recycling economy strategy of the current country is not met;
2. in the existing carbon dioxide trapping system, a simple absorption tower and a simple regeneration tower are basically adopted, and when the flue gas containing carbon dioxide enters the absorption tower and the regeneration tower for treatment, the gas is insufficiently contacted with the filler, so that incomplete gas treatment is easy to be caused, and energy consumption is also caused;
3. after the existing carbon dioxide trapping system is operated for a period of time, impurities are inevitably generated in the device, so that the problems of foaming and corrosion of the solution are easily caused, and the whole system is easily caused to be incapable of operating normally for a long time.
Accordingly, there is a need for improvements in the art to address the above-described problems.
Disclosure of Invention
The invention aims to provide the carbon dioxide trapping system for mineralized aerated block production, which can effectively reduce energy consumption and pollution, ensure long-time stable and normal operation of the whole system, and solve the problems that the existing carbon dioxide trapping system is serious in energy waste and the system cannot be operated stably and normally for a long time.
In order to solve the technical problems, the invention is realized by the following technical scheme:
the invention relates to a carbon dioxide trapping system for mineralized aerated block production, which comprises:
the inlet of the fan is used for absorbing carbon dioxide in the production process of the mineralized aerated block, and the outlet of the fan is used for conveying the carbon dioxide through a pipeline;
the washing liquid storage tank is used for storing desalted water or regenerated gas condensed water and adding a carbon dioxide absorbent; the air inlet at the lower end of the absorption tower is communicated with the outlet of the fan and is used for absorbing carbon dioxide, and the air outlet at the upper end of the absorption tower is communicated with the washing liquid storage tank and is used for conveying regenerated gas condensate water;
the lower end outlet of the regeneration tower is communicated with the first inlet of the lean-rich liquid heat exchanger through a rich liquid pump, the first outlet of the lean-rich liquid heat exchanger is communicated with the upper end inlet of the regeneration tower, the lower end outlet of the regeneration tower is communicated with the second inlet of the lean-rich liquid heat exchanger, and the second outlet of the lean-rich liquid heat exchanger is communicated with the upper end inlet of the absorption tower through a lean liquid pump and a lean liquid cooler;
the side outlet of the regeneration tower is communicated with the top end of the solution reboiler as soon as possible, the lower end outlet of the solution reboiler is communicated with the side inlet of the lower end of the regeneration tower, and the side inlet of the solution reboiler is communicated with the steam outer pipe;
the upper end outlet of the regeneration tower is communicated with the regeneration gas separator through a regeneration gas cooler, one group of outlets of the regeneration gas separator are used for discharging separated carbon dioxide, the other group of outlets of the regeneration gas separator are communicated with an underground tank and used for conveying other regeneration gas, and the underground tank is communicated with the upper end inlet of the regeneration tower through a reflux fluid supplementing pump;
wherein,,
carbon dioxide in the mineralized gas-adding block production process is sent into an absorption tower through a fan, flue gas flows from bottom to top and forms countercurrent contact with absorption liquid which enters the tower from the upper part through a washing liquid storage tank, so that CO2 is removed, and purified decarburized flue gas is discharged from an outlet of the tower top;
because the carbon dioxide absorbent has higher vapor pressure, in order to reduce the absorption liquid loss caused by the carrying-out of MEA vapor along with the flue gas, the absorption tower is generally divided into two sections, the lower section is used for acid gas absorption, and the upper section is used for reducing the vapor content of the carbon dioxide absorbent in the flue gas through water washing;
the washing water is recycled, along with continuous enrichment of the carbon dioxide absorbent in the washing water, the washing water is required to be merged into the rich liquid and sent to a regeneration tower for regeneration, so that the lost washing water is kept through regenerated gas condensed water, and meanwhile, the water balance of two sets of loops is ensured;
the absorbing liquid (rich liquid) absorbing the acid gas is pumped to a regeneration tower through a rich liquid pump, in order to reduce the consumption of steam during the regeneration of the rich liquid, the rich liquid is heated by using the waste heat of the regenerated absorbing solution (lean liquid), the purpose of cooling the regenerated solution is achieved, the rich liquid enters from the upper part of the regeneration tower, partial CO is stripped and desorbed, then enters a solution reboiler, CO2 in the rich liquid is further desorbed, lean liquid after CO2 desorption flows out from the bottom of the regeneration tower, and after heat exchange of a lean-rich liquid heat exchanger, the lean liquid enters a lean liquid cooler by pumping, and enters the absorption tower after cooling;
the solvent circulates back and forth to continuously absorb and desorb CO2, the CO and steam mixture coming out from the top of the regeneration tower is condensed by a regeneration gas cooler, the steam and water are separated by a regeneration gas separator, the condensed water returns to the system by a reflux liquid supplementing system, CO2 is separated, the gas enters an underground tank, and meanwhile, the gas in the underground tank can enter the regeneration tower for circulation separation.
Further, the carbon dioxide absorbent adopts a composite amine solution based on monoethanolamine, and is assisted by an antioxidant and a corrosion inhibitor.
Further, a pretreatment system can be arranged between the absorption tower and the fan, and the pretreatment system comprises a water spray cooling device and a cyclone separator.
Further, the absorption tower and the regeneration tower are both filled towers with small pressure drop and difficult foaming, pore plate corrugated fillers are arranged in the absorption tower and the regeneration tower, and high-efficiency silk screen foam removers are arranged at the top ends of the absorption tower and the regeneration tower.
Further, an air lifting cap is arranged at the bottom end of the regeneration tower.
Further, a lean liquid pipeline bypass between the lean liquid cooler and the absorption tower is provided with an activated carbon filter.
The invention has the following beneficial effects:
1. in the whole system, the composite amine solution based on monoethanolamine is adopted, and the antioxidant and the corrosion inhibitor are used as carbon dioxide absorbent, so that the high absorption capacity of the solution to CO2 is maintained, the regeneration energy consumption of the solution is reduced, and the equipment corrosion is reduced by utilizing the characteristics of high absorption rate, high absorption load and low regeneration energy consumption.
2. The absorption tower and the regeneration tower in the invention are both filled with the filler tower with small pressure drop and difficult foaming, and the pore plate corrugated filler is arranged in the absorption tower and the regeneration tower to ensure that the filler can uniformly pass through, the pressure drop is low, the circulation quantity is high, and the stable liquid film can be formed, so that the wetting rate is improved, and meanwhile, the air lift cap is arranged at the inner bottom end of the regeneration tower, so that the solution flowing down from the top of the regeneration tower is blocked by the air lift cap, and firstly, the solution completely enters the reboiler for full regeneration, thereby not only reducing the regeneration temperature, but also shortening the residence time of the solution in the reboiler, and reducing the degradation of the compound amine solution.
3. According to the invention, the active carbon filter is arranged on the lean solution pipeline bypass between the lean solution cooler and the absorption tower of the system, and the proportion of the solution passing through the active carbon filter is adjusted according to the pollution degree obtained by solution analysis so as to keep the solution clean, so that the system can normally and evenly run for a long time.
Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed for the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a process flow diagram of the system of the present invention.
In the drawings, the list of components represented by the various numbers is as follows:
1. a blower; 2. a washing liquid storage tank; 3. an absorption tower; 4. a lean solution cooler; 5. a lean liquid pump; 6. a rich liquid pump; 7. a lean rich liquid heat exchanger; 8. a regeneration tower; 9. a solution reboiler; 10. a regeneration gas cooler; 11. a regeneration gas separator; 12. an underground tank.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the present invention, it should be understood that the terms "open", "one side", "lower", "height", "in annular direction", "concentrically arranged", "alternately connected", "inner", "peripheral side", "outer side", etc. indicate orientation or positional relationship, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the components or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Referring to fig. 1, the invention is a carbon dioxide capturing system for mineralized aerated block production, comprising:
the inlet of the fan 1 is used for absorbing carbon dioxide in the production process of the mineralized aerated block, and the outlet of the fan 1 is used for conveying the carbon dioxide through a pipeline;
a washing liquid storage tank 2 for storing demineralized water or regenerated gas condensed water and adding a carbon dioxide absorbent;
the lower end air inlet of the absorption tower 3 is communicated with the outlet of the fan 1 and is used for absorbing carbon dioxide, and the upper end air outlet of the absorption tower is communicated with the washing liquid storage tank 2 and is used for conveying regenerated gas condensate water;
the lower end outlet of the absorption tower 3 is communicated with the first inlet of the lean-rich liquid heat exchanger 7 through the rich liquid pump 6, the first outlet of the lean-rich liquid heat exchanger 7 is communicated with the upper end inlet of the regeneration tower 8, the lower end outlet of the regeneration tower 8 is communicated with the second inlet of the lean-rich liquid heat exchanger 7, and the second outlet of the lean-rich liquid heat exchanger 7 is communicated with the upper end inlet of the absorption tower 3 through the lean liquid pump 5 and the lean liquid cooler 4;
the side outlet of the regeneration tower 8 is communicated with the top end of the solution reboiler 9 as soon as possible, the lower end outlet of the solution reboiler 9 is communicated with the side inlet of the lower end of the regeneration tower 8, and the side inlet of the solution reboiler 9 is communicated with the steam outer pipe;
the upper end outlet of the regeneration tower 8 is communicated with the regeneration gas separator 11 through a regeneration gas cooler 10, one group of outlets of the regeneration gas separator 11 are used for discharging separated carbon dioxide, the other group of outlets of the regeneration gas separator 11 are communicated with an underground tank 12 and used for conveying other regeneration gas, and the underground tank 12 is communicated with the upper end inlet of the regeneration tower 8 through a reflux liquid supplementing pump;
wherein,,
carbon dioxide in the mineralized gas-adding block production process is sent into an absorption tower 3 through a fan 1, flue gas flows from bottom to top and forms countercurrent contact with absorption liquid which enters the tower from the upper part through a washing liquid storage tank 2, so that CO2 is removed, and purified decarburized flue gas is discharged from an outlet of the tower top;
because the absorbent of carbon dioxide has higher vapor pressure, in order to reduce the absorption liquid loss caused by the vapor of MEA carried out along with the flue gas, the absorption tower 3 is generally divided into two sections, the lower section is used for acid gas absorption, and the upper section is used for reducing the vapor content of the absorbent of carbon dioxide in the flue gas through water washing;
the washing water is recycled, along with the continuous enrichment of the carbon dioxide absorbent in the washing water, the washing water is required to be merged into the rich liquid and sent to the regeneration tower 8 for regeneration, so that the lost washing water is kept through the regenerated gas condensate water, and the water balance of the two sets of loops is ensured;
the absorbing liquid (rich liquid) absorbing the acid gas is pressurized by a rich liquid pump 6 and sent to a regeneration tower 8, in order to reduce the consumption of steam during the regeneration of the rich liquid, the rich liquid is heated by the waste heat of the regenerated absorbing solution (lean liquid), meanwhile, the purpose of cooling the regenerated solution is achieved, the rich liquid enters from the upper part of the regeneration tower 8, the CO2 is desorbed by stripping part, then enters a solution reboiler 9, the CO2 in the rich liquid is further desorbed, the lean liquid after the CO2 desorption flows out from the bottom of the regeneration tower 8, and is pumped to a lean liquid cooler 4 after heat exchange by a lean-rich liquid heat exchanger 7, and enters the absorption tower 3 after cooling;
the solvent circulates back and forth to form continuous absorption and desorption of CO2, the mixture of CO and steam coming out of the top of the regeneration tower 8 is condensed by a regeneration gas cooler 10, steam-water separation is carried out by a regeneration gas separator 11, the condensed water is returned to the system by a reflux liquid supplementing system, CO2 is separated, gas enters an underground tank 12, and meanwhile, the gas in the underground tank 12 can enter the regeneration tower 8 for circulation separation.
Furthermore, the carbon dioxide absorbent adopts a composite amine solution based on monoethanolamine, and is assisted by an antioxidant and a corrosion inhibitor, wherein the molecular weight of the monoethanolamine is 61.08, the boiling point is 171CC, the solidifying point is 10.5CC, the vapor pressure is 47.99Pa (20 CC), and the solubility in water (20 CC) is full. The MEA has stronger alkalinity, and can quickly react with carbon dioxide in the flue gas to generate more stable carbamate at the temperature of 20-50 CC, so that the carbon dioxide in the flue gas is removed; when the temperature of the solution is raised to 105CC or higher, carbamate is decomposed to release carbon dioxide, the solution is regenerated, and the solution has the characteristics of high absorptivity, high absorption load and low regeneration energy consumption, so that the high absorption capacity of the solution on CO2 is maintained, the regeneration energy consumption of the solution is reduced, and the equipment corrosion is reduced;
further, a pretreatment system can be arranged between the absorption tower 3 and the fan 1, the pretreatment system comprises a water spraying cooling device and a cyclone separator, the temperature of the flue gas led from dust removal and desulfurization is 40-50 degrees, the flue gas is just at the ideal absorption temperature of MEA, in general, the flue gas subjected to dust removal and desulfurization is pressurized by the fan and directly enters the absorption tower 3 to absorb CO2, the fan 1 is pressurized to overcome the pressure drop generated when the gas passes through the absorption tower 3, when the flue gas temperature exceeds the temperature under the fluctuation of working conditions, a water spraying temperature reducing device arranged in front of the absorption tower 3 is started to reduce the temperature to below 50 degrees, and the cyclone separator is used for preventing the water carried in the flue gas from entering the trapping device to damage the water balance of the system and removing the water and solid particles in the flue gas after desulfurization of the front stage.
Furthermore, the absorption tower 3 and the regeneration tower 8 are filled with the filler tower which is small in pressure drop and difficult to foam, pore plate corrugated fillers are arranged in the absorption tower 3 and the regeneration tower 8, and high-efficiency silk screen foam removers are arranged at the top ends of the absorption tower 3 and the regeneration tower 8, so that gas-liquid two phases can uniformly pass through the filter tower, the pressure drop is low, the circulation quantity is high, a stable liquid film can be formed on the surface of the pore plate by the solution, the wetting rate is high, the mass transfer efficiency is high, the filter tower has good wetting property and self-distributing capacity, the gas-liquid distribution is uniform, the amplification effect is almost avoided, the filler is regularly arranged, no dead angle exists, the liquid film is thin, the liquid holdup is small, the manufacturing cost is low, and the arranged high-efficiency silk screen foam removers are used for improving the separation efficiency, improving the operation condition of equipment behind the tower, recovering expensive reaction solvent and reducing the pollution to the environment;
further, the bottom end of the inside of the regeneration tower 8 is provided with an air lifting cap, so that the solution flowing down from the top of the regeneration tower 8 is blocked by the air lifting cap, and the solution firstly enters the solution reboiler 9 for regeneration completely, thereby reducing the regeneration temperature, shortening the residence time of the solution in the solution reboiler 9 and reducing the degradation of the compound amine solution;
furthermore, the solution reboiler 9 adopts a vertical natural differential pressure reboiler, and combines the design of an ascending gas cap in the regeneration tower 10, so that the solution enters the bottom of the solution reboiler 9 from a higher position in the regeneration tower 8, the heated ascending gas mixture enters the bottom of the regeneration tower 8, the regenerated solution (gas) flows out from a higher position in the regeneration tower 8 and enters the tower from a lower position, the height difference is the power for promoting the solution to naturally flow in the solution reboiler 9, and the flow arrangement not only maintains the characteristics of compact structure and high heat transfer coefficient of the vertical reboiler, but also avoids the unstable problem of thermosiphon;
further, an active carbon filter is arranged on a lean solution pipeline bypass between the lean solution cooler 4 and the absorption tower 3, about 10% -15% of lean solution is filtered by the active carbon filter and the like, and the proportion of the solution passing through the active carbon filter is adjusted according to the pollution degree obtained by solution analysis so as to keep the solution clean, so that the system can be operated for a long time and efficiently without faults.
In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.

Claims (7)

1. A carbon dioxide capture system for mineralized aerated block production, comprising: the inlet of the fan (1) is used for absorbing carbon dioxide in the production process of the mineralized aerated block, and the outlet of the fan (1) is used for conveying the carbon dioxide through a pipeline;
a washing liquid storage tank (2) for storing demineralized water or regenerated gas condensed water and adding a carbon dioxide absorbent;
an air inlet at the lower end of the absorption tower (3) is communicated with an outlet of the fan (1) and is used for absorbing carbon dioxide, and an air outlet at the upper end of the absorption tower is communicated with the washing liquid storage tank (2) and is used for conveying regenerated gas condensate water;
the lower end outlet of the absorption tower (3) is communicated with the first inlet of the lean-rich liquid heat exchanger (7) through the rich liquid pump (6), the first outlet of the lean-rich liquid heat exchanger (7) is communicated with the upper end inlet of the regeneration tower (8), the lower end outlet of the regeneration tower (8) is communicated with the second inlet of the lean-rich liquid heat exchanger (7), and the second outlet of the lean-rich liquid heat exchanger (7) is communicated with the upper end inlet of the absorption tower (3) through the lean liquid pump (5) and the lean liquid cooler (4);
the side outlet of the regeneration tower (8) is communicated with the top end of the solution reboiler (9) as soon as possible, the lower end outlet of the solution reboiler (9) is communicated with the lower end side inlet of the regeneration tower (8), and the side inlet of the solution reboiler (9) is communicated with the steam outer pipe;
the upper end outlet of the regeneration tower (8) is communicated with the regeneration gas separator (11) through a regeneration gas cooler (10), one group of outlets of the regeneration gas separator (11) are used for discharging separated carbon dioxide, the other group of outlets of the regeneration gas separator (11) are communicated with the underground tank (12) and are used for conveying other regeneration gas, and the underground tank (12) is communicated with the upper end inlet of the regeneration tower (8) through a reflux liquid supplementing pump;
wherein,,
carbon dioxide in the mineralized gas-adding block production process is sent into an absorption tower (3) through a fan (1), flue gas flows from bottom to top and forms countercurrent contact with absorption liquid which enters the tower from the upper part through a washing liquid storage tank (2), so that CO2 is removed, and purified decarburized flue gas is discharged from an outlet of the tower top; because the absorbent of carbon dioxide has higher vapor pressure, in order to reduce the absorption liquid loss caused by the vapor of MEA carried out along with the flue gas, the absorption tower 3 is generally divided into two sections, the lower section is used for acid gas absorption, and the upper section is used for reducing the vapor content of the absorbent of carbon dioxide in the flue gas through water washing;
the washing water is recycled, along with the continuous enrichment of the carbon dioxide absorbent in the washing water, the washing water is required to be merged into the rich liquid and sent to a regeneration tower (8) for regeneration, so that the lost washing water is kept by the regenerated gas condensed water, and the water balance of two sets of loops is ensured;
the absorbing solution (rich solution) absorbing the acid gas is pressurized and sent to a regeneration tower (8) through a rich solution pump (6), in order to reduce the consumption of steam during the regeneration of the rich solution, the rich solution is heated by using the waste heat of the regenerated absorbing solution (lean solution), meanwhile, the purpose of cooling the regenerated solution is achieved, the rich solution enters from the upper part of the regeneration tower (8), the CO2 is desorbed through stripping, then enters a solution reboiler (9), the CO2 in the rich solution is further desorbed, the lean solution after the CO2 desorption flows out from the bottom of the regeneration tower (8), and is pumped to a lean solution cooler (4) after heat exchange of the lean solution heat exchanger (7), and enters the absorption tower (3) after cooling;
the solvent circulates back and forth to continuously absorb and desorb CO2, the mixture of CO and steam coming out of the top of the regeneration tower (10) is condensed by the regeneration gas cooler (10), steam-water separation is carried out by the regeneration gas separator (11), the condensed water returns to the system by the reflux liquid supplementing, CO2 is separated, gas enters the underground tank (12), and meanwhile, the gas in the underground tank (12) can enter the regeneration tower (10) for circulation separation.
2. The carbon dioxide capture system for mineralized aerated block production of claim 1, wherein the carbon dioxide absorbent is a monoethanolamine-based complex amine solution, supplemented with antioxidants and corrosion inhibitors.
3. A carbon dioxide capturing system for mineralized aerated block production according to claim 1, characterized in that a pretreatment system can be arranged between the absorption tower (3) and the fan (1), and the pretreatment system comprises a water spraying cooling device and a cyclone separator.
4. The carbon dioxide capturing system for mineralized aerated block production according to claim 1, wherein the absorption tower (3) and the regeneration tower (10) are filled with a filler tower with small pressure drop and difficult foaming, pore plate corrugated fillers are arranged in the absorption tower (3) and the regeneration tower (10), and high-efficiency silk screen foam removers are arranged at the top ends of the absorption tower (3) and the regeneration tower (10).
5. A carbon dioxide capturing system for mineralized aerated block production according to claim 1, characterized in that the inside bottom end of the regeneration tower (10) is provided with an air lifting cap.
6. A carbon dioxide capture system for mineralized aerated block production as claimed in claim 1, wherein the solution reboiler (9) is a vertical natural differential pressure reboiler.
7. A carbon dioxide capture system for mineralized aerated block production according to claim 1, characterized in that the lean liquor piping bypass between the lean liquor cooler (4) and the absorption tower (3) is provided with an activated carbon filter.
CN202310108272.2A 2023-02-14 2023-02-14 Carbon dioxide trapping system for mineralized aerated block production Pending CN116196726A (en)

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