CN112221327A - Carbon dioxide ammonia capture and low-temperature liquefaction system and method for coal-fired power plant - Google Patents
Carbon dioxide ammonia capture and low-temperature liquefaction system and method for coal-fired power plant Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 37
- ZEYWAHILTZGZBH-UHFFFAOYSA-N azane;carbon dioxide Chemical compound N.O=C=O ZEYWAHILTZGZBH-UHFFFAOYSA-N 0.000 title claims description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 290
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 148
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 148
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 131
- 238000010521 absorption reaction Methods 0.000 claims abstract description 90
- 239000007788 liquid Substances 0.000 claims abstract description 83
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 37
- 238000003795 desorption Methods 0.000 claims abstract description 30
- 230000002745 absorbent Effects 0.000 claims abstract description 18
- 239000002250 absorbent Substances 0.000 claims abstract description 18
- 238000004064 recycling Methods 0.000 claims abstract description 15
- 239000000126 substance Substances 0.000 claims abstract description 14
- 230000000694 effects Effects 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 83
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 29
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 12
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 11
- 239000001099 ammonium carbonate Substances 0.000 claims description 10
- 238000001514 detection method Methods 0.000 claims description 9
- 238000005057 refrigeration Methods 0.000 claims description 9
- 239000007791 liquid phase Substances 0.000 claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 235000012501 ammonium carbonate Nutrition 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 5
- 238000004458 analytical method Methods 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 2
- 230000023556 desulfurization Effects 0.000 claims description 2
- 230000009467 reduction Effects 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 claims description 2
- PRKQVKDSMLBJBJ-UHFFFAOYSA-N ammonium carbonate Chemical class N.N.OC(O)=O PRKQVKDSMLBJBJ-UHFFFAOYSA-N 0.000 claims 1
- 239000003245 coal Substances 0.000 claims 1
- 239000000243 solution Substances 0.000 description 11
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 4
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 4
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 235000019688 fish Nutrition 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 235000013372 meat Nutrition 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/79—Injecting reactants
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
- F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The invention provides a system and a method for capturing and liquefying carbon dioxide in a coal-fired power plant by an ammonia-process, which comprises a carbon dioxide chemical method capturing system, a low-temperature liquefying system and an absorbent recycling system, wherein the carbon dioxide chemical method capturing system comprises a carbon dioxide absorption tower, an ammonia absorption tower and a carbon dioxide desorption tower; the low-temperature liquefaction system comprises an airflow dryer, a gas booster, a screw compressor, a condenser and an evaporator; the absorbent recycling part comprises a gas-liquid separator, a throttle valve, a liquid one-way valve, a gas one-way valve, a liquid ammonia storage tank and a liquid ammonia evaporator. The invention has the characteristics of efficiently capturing carbon dioxide, reducing greenhouse effect and protecting environment, and can be widely applied to various coal-fired power plants and related coal-fired industry industries.
Description
Technical Field
The invention relates to the field of resource environment, in particular to a system and a method for capturing carbon dioxide by an ammonia process and liquefying at low temperature for a coal-fired power plant.
Background
At present, the greenhouse effect is becoming more serious, carbon dioxide is the main component of the greenhouse effect, and how to reduce the emission of the carbon dioxide becomes a problem to be solved urgently. For China, the annual emission of carbon dioxide exceeds 100 hundred million tons, wherein about half of the emission is from the emission after combustion of a coal-fired power plant, and based on China, the main reason is that thermal power generation is adopted, so that the carbon dioxide is continuously increased at a high speed increase before 2030 years. Carbon dioxide generated by a thermal power plant is directly discharged into the atmosphere, only the greenhouse effect is intensified, and serious damage is caused to global climate and human living space; carbon dioxide is a main greenhouse gas, but is also a potential carbon resource, and has extremely wide application, for example, the production rate of petroleum can be improved by injecting carbon dioxide into an oil well, and liquid carbon dioxide is a natural refrigerating working medium; in addition, the carbon dioxide collecting and liquefying device is used for keeping fruits, vegetables and fish meat fresh in the food industry and is a basic resource in the chemical industry, so that the carbon dioxide discharged is particularly important to be effectively collected and utilized, and a technology for collecting and liquefying the carbon dioxide discharged by a coal-fired power plant is particularly needed.
At present, many enterprises and institutions at home and abroad have started research on carbon dioxide collection technology, and as for 8 months in 2018, 37 large-scale CCUS projects are provided all over the world, wherein 22 projects are in operation or construction stages, and the comprehensive CAPTURE can meet the defects, such as carbon dioxide CAPTURE equipment DIRECT AIR CAPTURE manufactured by two engineers in Switzerland Crisebofu and Wutzench, which can CAPTURE carbon dioxide from the atmosphere, but the equipment is low in efficiency due to low concentration of carbon dioxide in the atmosphere. The MEA solution is used for absorbing carbon dioxide, which is a mature process at the present stage, but the MEA solution needs a high temperature of more than 110 ℃ during analysis, so that the energy consumption is large, and the collected substances are gas phases, which are not favorable for storage and transportation. The membrane separation method has problems that the gas separation membrane has poor selectivity to gas and is easily corroded.
Therefore, the method for capturing and liquefying carbon dioxide discharged by a coal-fired power plant has the advantages of large energy consumption, low efficiency and difficult transportation of captured products in the prior art, and has important practical significance for the problems and the prior art.
Disclosure of Invention
The invention aims to provide a carbon dioxide ammonia method capturing and low-temperature liquefying system for a coal-fired power plant, which can reduce the harmful effect caused by excessive carbon dioxide discharged into the atmosphere, relieve the greenhouse effect and serve the production and life of people by taking liquid carbon dioxide generated by the system as a resource.
The technical scheme adopted by the invention is as follows:
a carbon dioxide ammonia method capturing and low-temperature liquefying system of a coal-fired power plant comprises a carbon dioxide chemical method capturing system, a low-temperature liquefying system and an absorbent recycling system; the carbon dioxide chemical method capturing system comprises a carbon dioxide absorption tower, an ammonia absorption tower and a carbon dioxide desorption tower which are connected in sequence; the carbon dioxide desorption tower separates ammonia gas and carbon dioxide from the discharged waste gas through a low-temperature liquefaction system, and the ammonia gas enters an absorbent recycling system and plays a role in a carbon dioxide chemical method capturing system again.
Further, the carbon dioxide absorption tower comprises an ammonia water storage tank outside the tower; the ammonia water storage tank outside the tower is connected with a first spray nozzle in the tower; the air inlet pipeline is connected with an air inlet at the middle part of the carbon dioxide absorption tower; a first liquid storage tank in the carbon dioxide absorption tower is arranged at the bottom of the carbon dioxide absorption tower, an inclined first inclined plane is arranged at the bottom of the liquid storage tank in the first tower, and a first pipeline arranged on the first inclined plane leads to a third liquid storage tank in the carbon dioxide desorption tower; the top of the carbon dioxide absorption tower is provided with a first gas outlet, and the first gas outlet is connected to a second gas inlet in the middle of the ammonia absorption tower through a gas transmission pipeline.
Further, the ammonia absorption tower comprises an external tower water storage tank; the tower external water storage tank is connected with a second spray nozzle in the tower; a liquid storage tank in a second tower is arranged at the bottom of the ammonia absorption tower, a water inlet pipeline is connected above the liquid storage tank in the second tower, and the bottom of the liquid storage tank in the second tower is a second inclined plane; a second pipeline is arranged on the second inclined plane and connected with an ammonia water storage tank outside the carbon dioxide absorption tower; the tower top of the ammonia absorption tower is a second air outlet; a second electromagnetic cut-off valve is arranged on the second air outlet, and a first gas one-way valve and a first electromagnetic cut-off valve are transversely arranged between the second electromagnetic cut-off valve and the second air outlet and are connected with a second air inlet; the first electromagnetic cut-off valve and the second electromagnetic cut-off valve are controlled by a wall-mounted ammonia gas detection sensor arranged at the second gas outlet.
Further, a liquid storage tank in a third tower is arranged in the carbon dioxide desorption tower, the liquid storage tank in the third tower is divided into two parts, and liquid levels of the two parts are detected and adjusted through a liquid level controller; the reboiler and the liquid delivery pump are arranged outside the carbon dioxide desorption tower; a cooler is arranged outside a third air outlet at the top of the tower; and the pipeline connected with the carbon dioxide desorption tower is connected with the ammonia water storage tank outside the carbon dioxide absorption tower and is used for conveying the solution with lower solute concentration after analysis to the ammonia water storage tank again and reusing the solution.
Furthermore, rotational flow demisting layers are arranged below the air outlets of the carbon dioxide absorption tower, the ammonia gas absorption tower and the carbon dioxide desorption tower and are used for removing water vapor generated in the absorption tower in the absorption process.
Further, the low-temperature liquefaction system comprises a gas flow dryer, a gas booster, a screw compressor, a condenser and an evaporator; the air flow dryer is respectively connected with the cooler and the gas booster compressor, the gas booster compressor is connected at a gas inlet at one end of the gas-liquid separator through the first condenser, one end of the evaporator and the screw compressor are respectively connected at a gas outlet at one end of the gas-liquid separator, and the other end of the screw compressor is connected at the evaporator through the second condenser.
Further, the absorbent recycling system comprises a gas-liquid separator, a throttle valve, a liquid one-way valve, a liquid ammonia storage tank, a liquid ammonia evaporator and a second gas one-way valve; and the gas-liquid separation is sequentially connected with a throttle valve, a liquid one-way valve, a liquid ammonia storage tank and a liquid ammonia evaporator and is connected with the ammonia water storage tank outside the tower again through a second gas one-way valve.
The trapping and liquefying method carried out by adopting the invention comprises the following steps:
firstly, enabling flue gas of a coal-fired power plant to enter a carbon dioxide absorption tower after desulfurization, denitrification and dedusting of the power plant, and fully spraying carbon dioxide at normal temperature and normal pressure to be absorbed by ammonia water with the concentration of 7%;
secondly, the gas absorbed by the carbon dioxide absorption tower enters an ammonia absorption tower, and the ammonia absorption tower takes water as an absorbent and completely absorbs ammonia after full spraying;
thirdly, the saturated ammonium carbonate solution generated in the carbon dioxide absorption tower enters a carbon dioxide desorption tower, the ammonium carbonate solution is heated to 90 ℃ and is heated and decomposed to generate a mixed gas of carbon dioxide, ammonia and water vapor, and the water vapor is removed through a cooler;
fourthly, the mixed gas without the water vapor enters a supercharger to be pressurized to 1.9MPa, the pressurized gas enters a first condenser, the mixed gas is cooled to 30 ℃ in the first condenser, the ammonia gas is completely liquefied, after passing through a gas-liquid separator, the carbon dioxide gas with normal temperature and high pressure enters a low-temperature liquefaction system, and the liquid ammonia enters an absorbent recycling system through the gas-liquid separator;
fifthly, a screw compressor in the low-temperature liquefaction system sucks the gaseous refrigeration working medium from the evaporator, compresses the gaseous refrigeration working medium to a condensation pressure, and then discharges the gaseous refrigeration working medium to a second condenser; the refrigerant after being condensed in the second condenser becomes a liquid phase; then the liquid-phase working medium enters a thermostatic expansion valve for pressure reduction; the gas-liquid two-phase coexisting working medium after being throttled and decompressed by the thermostatic expansion valve enters the evaporator, and exchanges energy with gas-phase carbon dioxide in the evaporator so as to achieve the effect of cooling the cooled substance.
The invention has the following beneficial effects:
(1) the concentration of carbon dioxide in the flue gas of the coal-fired power plant is higher than that of carbon dioxide in the atmosphere, so that the carbon dioxide is a better source for capturing carbon dioxide at present, the carbon dioxide capturing cost is easier to reduce, and the efficiency is improved;
(2) absorbing carbon dioxide in the flue gas by using ammonia water with lower desorption temperature, absorbing and purifying ammonia gas in a carbon dioxide absorption tower, and efficiently recycling and reusing ammonia gas generated by decomposition in the carbon dioxide desorption tower;
(3) effectively combines the trapping method and the liquefying method, and avoids the resource waste caused by trapping only by one method in the prior art.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention;
FIG. 2 is a schematic view showing the structure of a carbon dioxide absorption tower according to the present invention;
FIG. 3 is a schematic view of the structure of an ammonia absorption tower according to the present invention;
FIG. 4 is a schematic view showing the structure of a carbon dioxide stripping column according to the present invention;
FIG. 5 is a schematic diagram of the cryogenic liquefaction system of the present invention;
in the figure: 3-air inlet pipeline, 4-first air outlet, 5-first spray nozzle, 6-outer ammonia water storage tank, 7-first absorption tower window, 8-first air inlet, 9-first inclined plane, 10-air transmission pipeline, 12-first pipeline, 13-second air outlet, 14-second spray nozzle, 15-second absorption tower window, 16-second air inlet, 17-outer water storage tank, 18-carbon dioxide desorption tower, 19-reboiler, 20-liquid delivery pump, 21-support seat, 22-circulating cooling water outlet, 23-cooler, 24-circulating cooling water inlet, 25-gas booster, 26-first condenser, 27-screw compressor, 28-second condenser, 29-thermal expansion valve, 30-evaporator, 31-carbon dioxide pipeline, 32-liquid level controller, 33-liquid storage tank in third tower, 34-carbon dioxide absorption tower, 35-ammonia absorption tower, 36-first water pump, 37-first liquid storage tank, 38-second inclined plane, 39-liquid storage tank in second tower, 40-third air outlet, 41-water inlet pipeline, 42-second pipeline, 43-first cyclone defogging layer, 44-second cyclone defogging layer, 45-third cyclone defogging layer, 46-ammonia detection sensor, 47-first gas one-way valve, 48-first electromagnetic cut-off valve, 49-second electromagnetic cut-off valve, 50-second water pump, 51-gas-liquid separator, 52-third pipeline, 53-throttle valve, 54-liquid one-way valve, 55-liquid ammonia storage tank, 56-liquid ammonia evaporator, 57-second gas one-way valve and 58-airflow dryer.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.
The invention relates to a carbon dioxide ammonia method capturing and low-temperature liquefying system of a coal-fired power plant, which comprises a carbon dioxide chemical method capturing system, a low-temperature liquefying system and an absorbent recycling system. As shown in fig. 1, the carbon dioxide chemical method capturing system comprises a carbon dioxide absorption tower, an ammonia absorption tower and a carbon dioxide desorption tower which are connected in sequence through pipelines; the low-temperature liquefaction system comprises a drying part, a pressurization part, a power part, a heat exchange part and a pressure regulation part; the drying part is a gas flow dryer, the pressurizing part is a gas booster and is used for increasing the pressure of the carbon dioxide gas so that the carbon dioxide gas reaches a liquid phase saturation point at a certain temperature; the power part is a screw compressor and is used for compressing a refrigerating working medium, the heat exchange part comprises a condenser and an evaporator, and the pressure adjusting part is a thermal expansion valve and is arranged between the condenser and the evaporator. The absorbent recycling system comprises a gas-liquid separation part, a pressure adjusting part, a flow direction control part, a liquid ammonia storage part and a liquid ammonia vaporization part. The gas-liquid separation part is a gas-liquid separator, the pressure regulation part is a throttle valve, the flow direction control part is a liquid one-way valve and a gas one-way valve, the liquid ammonia storage part is a liquid ammonia storage tank, and the liquid ammonia vaporization part is a liquid ammonia evaporator.
As shown in fig. 2, the carbon dioxide absorption tower 34 includes an ammonia water storage tank 6 outside the tower, and the ammonia water in the ammonia water storage tank 6 outside the tower is sprayed out from the first spray nozzle 5 through a pipeline by a first water pump 36 driving the ammonia water to flow. The first spray nozzle 5 is arranged in the middle of the carbon dioxide absorption tower 34 and is provided with a plurality of layers, ammonia water reacts with carbon dioxide in the discharged flue gas to generate a mixed solution of ammonium carbonate and ammonium bicarbonate, so that gaseous carbon dioxide is fixed. The bottom of the carbon dioxide absorption tower 34 is provided with a first in-tower liquid storage tank 37 for storing the mixed solution of ammonium carbonate and ammonium bicarbonate generated by the reaction. At the bottom of the liquid storage tank 37 in the first tower is a first slope 9 having an inclination of 5 deg. for preventing the absorption liquid from remaining when the absorption tower is emptied. The rich liquid generated by the reaction in the column flows into a third column liquid storage tank 33 in the carbon dioxide desorption column 18 through a first pipe 12 to be treated next. The gas inlet pipe 3 is connected to the gas inlet 8 in the middle of the carbon dioxide absorption tower 34. The top of the carbon dioxide absorption tower 34 is provided with a first gas outlet 4, and the first gas outlet 4 is connected with a second gas inlet 16 in the middle of the ammonia absorption tower through a gas transmission pipeline 10. A first cyclone demisting layer 43 is arranged below the first air outlet 4 of the carbon dioxide absorption tower 34 to remove water vapor generated in the absorption tower due to the absorption process. The carbon dioxide absorption tower 34 is externally provided with a first absorption tower window 7. The first spray nozzle 5 and the pipeline connected with the ammonia water storage tank 6 are steel linings and have good corrosion resistance.
As shown in fig. 3, the ammonia gas absorption tower 35 has a structure similar to that of the carbon dioxide absorption tower 34, and includes an external water storage tank 17, a second water pump 50 for driving water to flow, and a second spray nozzle 14 provided in the tower. The second spray nozzle 14 is provided with a plurality of layers and is connected with an external tower water storage tank 17 through a second water pump 50; the bottom of the ammonia absorption tower 35 is provided with a second tower inner liquid storage tank 39, a water inlet pipeline 41 is connected above the second tower inner liquid storage tank 39, and the bottom of the second tower inner liquid storage tank 39 is a second inclined plane 38 with an angle of 5 degrees. And a second absorption tower window 15 is arranged outside the ammonia absorption tower 35, a second air inlet 16 is arranged in the middle of the tower, and a second air outlet 13 and a second cyclone defogging layer 44 close to the top of the tower are arranged on the top of the tower. A wall-mounted ammonia gas detection sensor 46 is installed at the second air outlet 13, a first electromagnetic shut-off valve 48 and a second electromagnetic shut-off valve 49 controlled by the ammonia gas detection sensor 46 are arranged above the ammonia gas detection sensor 46 of the ammonia gas absorption tower, and a first gas one-way valve 47 connected with the first electromagnetic shut-off valve 48 through a pipeline is arranged above the ammonia gas detection sensor 46.
In the invention, ammonia gas is purified by adopting a method of absorption by an absorption tower at normal temperature and normal pressure, a second electromagnetic cut-off valve 49 controlled by an ammonia gas detection sensor 46 is opened when the gas after absorption and purification reaches the emission standard, and a first electromagnetic cut-off valve 48 is closed; the first electromagnetic cut-off valve 48 controlled by the ammonia gas detection sensor 46 is opened when the gas after absorption and purification does not reach the emission standard, and the second electromagnetic cut-off valve 49 is closed. The first gas check valve 47 connected to the first electromagnetic cut-off valve 48 via a pipeline is always in an open state, and functions such that gas can only flow from the first electromagnetic cut-off valve 48 to the gas pipeline 10, and gas in the gas pipeline 10 is not directly discharged to the atmosphere before absorption and purification, so that the discharged gas reaches the emission standard. In the present invention, water is selected as the absorbent, and when the concentration of the solute in the absorbent water reaches a certain value, a proper amount of ammonia gas is introduced into the solution to make it become an ammonia water solution with a concentration of 7%, and the ammonia water solution is transported to the ammonia water storage tank 6 outside the carbon dioxide absorption tower 34 through the second pipe 42.
As shown in FIG. 4, a third in-tower liquid storage tank 33 is provided in the carbon dioxide desorption tower 18, and a third swirling defogging layer 45 and a third air outlet 40 are provided at the top. The liquid storage tank 33 in the third column is divided into two parts, and the liquid levels of the two parts are detected and adjusted by the liquid level controller 32, so that the danger caused by the overhigh liquid level on one side is prevented. A reboiler 19 is installed outside the carbon dioxide desorption tower 18 for decomposing the mixed solution of ammonium carbonate and ammonium bicarbonate by heating, thereby reforming carbon dioxide into a gaseous state. The reboiler 19 is connected with a liquid transfer pump 20 for providing pressure and power to the ammonium carbonate and ammonium bicarbonate in the transfer so as to make the mixed solution continuously and stably flow. A cooler 23 is installed outside the third gas outlet 40, the cooler 23 is used for cooling the mixed gas of carbon dioxide, ammonia gas and water vapor generated in the carbon dioxide desorption tower 18, and the cooler 23 is provided with a circulating cooling water outlet 22 and a circulating cooling water inlet 24, that is, the cooler 23 adopts a water cooling mode. The pipeline 11 connected with the carbon dioxide desorption tower 18 is connected with the ammonia water holding tank 6 outside the carbon dioxide absorption tower, and is used for conveying the solution with lower solute concentration after analysis to the ammonia water holding tank 6 again for reuse.
The carbon dioxide absorption tower 34, the ammonia absorption tower 35 and the carbon dioxide desorption tower 18 are all arranged on the supporting seat 21, and the supporting seat 21 is of a common concrete structure and has stronger bearing capacity so as to improve the height of the tower and prevent the tower from being damaged by external factors during operation.
As shown in fig. 5, the low-temperature liquefaction system employs a single-stage mechanical compression refrigeration cycle, and the refrigerant undergoes heat exchange in the liquid ammonia evaporator 56 to absorb heat and become a gas. After passing through the dryer 58, the mixed gas of ammonia gas and carbon dioxide generated by the carbon dioxide desorption tower 18 is pressurized to 1.9Mpa by the booster 25, which is used to increase the pressure of the carbon dioxide gas and ammonia gas to reach the liquid phase saturation point at a certain temperature, and then enters the first condenser 26; the ammonia gas is liquefied by cooling the gas to 30 c by condensation in condenser 26. Liquefied liquid ammonia and pure carbon dioxide are separated through a gas-liquid separator 51, the liquid ammonia enters a third pipeline 52, is throttled and depressurized through a throttle valve 53, then flows into a liquid ammonia storage tank 55 through a liquid one-way valve 54, the liquid ammonia flowing out of the liquid ammonia storage tank 55 is gasified through a liquid ammonia evaporator 56, and the gasified ammonia enters an ammonia water storage tank 6 through a second gas one-way valve 57, so that the recycling of absorbent solutes is realized.
The refrigerant R134a enters the screw compressor 27 through a pipeline, is compressed into high-temperature and high-pressure gas, enters the second condenser 28 through a pipeline and is cooled into refrigerant liquid; the liquid of the refrigerant R134a enters the thermostatic expansion valve 29, under the action of the thermostatic expansion valve 29, the liquid pressure of the refrigerant R134a is reduced from the condensation pressure to the evaporation pressure, and meanwhile, a part of the refrigerant is converted into steam; the other part of the liquid refrigerant R134a enters the refrigerant pipe of the evaporator 30 to exchange heat, thereby completing a refrigeration cycle. The carbon dioxide separated from the gas-liquid separator 51 at a pressure of 1.9MPa is introduced into the evaporator 30 at a refrigeration temperature of-24 ℃ through the carbon dioxide line 31, and at a temperature of-24 ℃ and a pressure of 1.9MPa, the carbon dioxide is in a liquid phase, so that high-concentration liquid carbon dioxide is obtained, and the liquid carbon dioxide can be stored in a pressure-resistant steel cylinder.
During operation, flue gas discharged by a coal-fired power plant enters a carbon dioxide absorption tower after being dedusted and cooled, and carbon dioxide is absorbed by an absorbent in the carbon dioxide absorption tower to obtain an absorption liquid with higher concentration; the unabsorbed gas and a small amount of volatilized ammonia gas are introduced into an ammonia gas absorption tower to be purified, the gas which reaches the emission standard after purification is discharged into the atmosphere, the absorption liquid with higher concentration obtained from the carbon dioxide absorption tower is introduced into a desorption tower to be regenerated by carbon dioxide, and carbon dioxide gas and ammonia gas are obtained from the desorption tower; pressurizing carbon dioxide gas and ammonia to 1.9MPa and cooling to 30 ℃ and then obtaining liquid ammonia and carbon dioxide gas, liquid ammonia and carbon dioxide gas enter a gas-liquid separator to separate, the obtained carbon dioxide gas is transported to a low-temperature liquefaction system through a pipeline to be liquefied, the liquid ammonia is depressurized through a throttle valve, the liquid after depressurization enters a liquid ammonia storage tank through a liquid one-way valve to be temporarily stored, the liquid ammonia flowing out of the liquid ammonia storage tank enters a liquid ammonia vaporizer to be vaporized, the obtained gas enters an ammonia water storage tank arranged outside a carbon dioxide absorption tower through a gas one-way valve, and therefore ammonia recycling is achieved.
Claims (8)
1. A coal fired power plant carbon dioxide ammonia process entrapment and low temperature liquefaction system which characterized in that: the system comprises a carbon dioxide chemical method capturing system, a low-temperature liquefying system and an absorbent recycling system; the carbon dioxide chemical method capturing system comprises a carbon dioxide absorption tower, an ammonia absorption tower and a carbon dioxide desorption tower which are connected in sequence; the carbon dioxide desorption tower separates ammonia gas and carbon dioxide from the discharged waste gas through a low-temperature liquefaction system, and the ammonia gas enters an absorbent recycling system and plays a role in a carbon dioxide chemical method capturing system again.
2. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: the carbon dioxide absorption tower comprises an ammonia water storage tank outside the tower; the ammonia water storage tank outside the tower is connected with a first spray nozzle in the tower; the air inlet pipeline is connected with an air inlet at the middle part of the carbon dioxide absorption tower; a first liquid storage tank in the carbon dioxide absorption tower is arranged at the bottom of the carbon dioxide absorption tower, an inclined first inclined plane is arranged at the bottom of the liquid storage tank in the first tower, and a first pipeline arranged on the first inclined plane leads to a third liquid storage tank in the carbon dioxide desorption tower; the top of the carbon dioxide absorption tower is provided with a first gas outlet, and the first gas outlet is connected to a second gas inlet in the middle of the ammonia absorption tower through a gas transmission pipeline.
3. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: the ammonia absorption tower comprises an external tower water storage tank; the tower external water storage tank is connected with a second spray nozzle in the tower; a liquid storage tank in a second tower is arranged at the bottom of the ammonia absorption tower, a water inlet pipeline is connected above the liquid storage tank in the second tower, and the bottom of the liquid storage tank in the second tower is a second inclined plane; a second pipeline is arranged on the second inclined plane and connected with an ammonia water storage tank outside the carbon dioxide absorption tower; the tower top of the ammonia absorption tower is a second air outlet; a second electromagnetic cut-off valve is arranged on the second air outlet, and a first gas one-way valve and a first electromagnetic cut-off valve are transversely arranged between the second electromagnetic cut-off valve and the second air outlet and are connected with a second air inlet; the first electromagnetic cut-off valve and the second electromagnetic cut-off valve are controlled by a wall-mounted ammonia gas detection sensor arranged at the second gas outlet.
4. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: a liquid storage tank in a third tower is arranged in the carbon dioxide desorption tower, the liquid storage tank in the third tower is divided into two parts, and the liquid levels of the two parts are detected and adjusted through a liquid level controller; the reboiler and the liquid delivery pump are arranged outside the carbon dioxide desorption tower; a cooler is arranged outside a third air outlet at the top of the tower; and the pipeline connected with the carbon dioxide desorption tower is connected with the ammonia water storage tank outside the carbon dioxide absorption tower and is used for conveying the solution with lower solute concentration after analysis to the ammonia water storage tank again and reusing the solution.
5. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: and cyclone defogging layers are arranged below the air outlets of the carbon dioxide absorption tower, the ammonia gas absorption tower and the carbon dioxide desorption tower and are used for removing water vapor generated in the absorption tower in the absorption process.
6. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: the low-temperature liquefaction system comprises a gas flow dryer, a gas booster, a screw compressor, a condenser and an evaporator; the air flow dryer is respectively connected with the cooler and the gas booster compressor, the gas booster compressor is connected at a gas inlet at one end of the gas-liquid separator through the first condenser, one end of the evaporator and the screw compressor are respectively connected at a gas outlet at one end of the gas-liquid separator, and the other end of the screw compressor is connected at the evaporator through the second condenser.
7. The system for capturing and liquefying carbon dioxide by ammonia process in coal-fired power plant according to claim 1, characterized in that: the absorbent recycling system comprises a gas-liquid separator, a throttle valve, a liquid one-way valve, a liquid ammonia storage tank, a liquid ammonia evaporator and a second gas one-way valve; and the gas-liquid separation is sequentially connected with a throttle valve, a liquid one-way valve, a liquid ammonia storage tank and a liquid ammonia evaporator and is connected with the ammonia water storage tank outside the tower again through a second gas one-way valve.
8. A carbon dioxide ammonia method capturing method for a coal-fired power plant is characterized by comprising the following steps:
firstly, enabling flue gas of a coal-fired power plant to enter a carbon dioxide absorption tower after desulfurization, denitrification and dedusting of the power plant, and fully spraying carbon dioxide at normal temperature and normal pressure to be absorbed by ammonia water with the concentration of 7%;
secondly, the gas absorbed by the carbon dioxide absorption tower enters an ammonia absorption tower, and the ammonia absorption tower takes water as an absorbent and completely absorbs ammonia after full spraying;
thirdly, the saturated ammonium carbonate solution generated in the carbon dioxide absorption tower enters a carbon dioxide desorption tower, the ammonium carbonate solution is heated to 90 ℃ and is heated and decomposed to generate a mixed gas of carbon dioxide, ammonia and water vapor, and the water vapor is removed through a cooler;
fourthly, the mixed gas without the water vapor enters a supercharger to be pressurized to 1.9MPa, the pressurized gas enters a first condenser, the mixed gas is cooled to 30 ℃ in the first condenser, the ammonia gas is completely liquefied, after passing through a gas-liquid separator, the carbon dioxide gas with normal temperature and high pressure enters a low-temperature liquefaction system, and the liquid ammonia enters an absorbent recycling system through the gas-liquid separator;
fifthly, a screw compressor in the low-temperature liquefaction system sucks the gaseous refrigeration working medium from the evaporator, compresses the gaseous refrigeration working medium to a condensation pressure, and then discharges the gaseous refrigeration working medium to a second condenser; the refrigerant after being condensed in the second condenser becomes a liquid phase; then the liquid-phase working medium enters a thermostatic expansion valve for pressure reduction; the gas-liquid two-phase coexisting working medium after being throttled and decompressed by the thermostatic expansion valve enters the evaporator, and exchanges energy with gas-phase carbon dioxide in the evaporator so as to achieve the effect of cooling the cooled substance.
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| CN115869751A (en) * | 2021-09-29 | 2023-03-31 | 中国石油化工股份有限公司 | Treatment of a gas containing H 2 S and CO 2 Of (2) a gas |
| CN117861425A (en) * | 2024-02-04 | 2024-04-12 | 江苏三吉利化工股份有限公司 | Treatment system and method for zero emission of furan phenol etherification waste gas |
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