CN116785905A - Carbon capturing system and carbon capturing method by circulating ammonia method - Google Patents
Carbon capturing system and carbon capturing method by circulating ammonia method Download PDFInfo
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- CN116785905A CN116785905A CN202310227892.8A CN202310227892A CN116785905A CN 116785905 A CN116785905 A CN 116785905A CN 202310227892 A CN202310227892 A CN 202310227892A CN 116785905 A CN116785905 A CN 116785905A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 44
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 35
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 113
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 91
- 230000008929 regeneration Effects 0.000 claims abstract description 65
- 238000011069 regeneration method Methods 0.000 claims abstract description 65
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 54
- 238000010521 absorption reaction Methods 0.000 claims abstract description 51
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000003546 flue gas Substances 0.000 claims abstract description 49
- 239000007789 gas Substances 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 47
- 239000013078 crystal Substances 0.000 claims abstract description 46
- 238000001816 cooling Methods 0.000 claims abstract description 44
- 238000007906 compression Methods 0.000 claims abstract description 36
- 230000006835 compression Effects 0.000 claims abstract description 36
- 230000002745 absorbent Effects 0.000 claims abstract description 32
- 239000002250 absorbent Substances 0.000 claims abstract description 32
- 238000004064 recycling Methods 0.000 claims abstract description 18
- 239000002918 waste heat Substances 0.000 claims abstract description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 44
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 31
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 30
- 239000001569 carbon dioxide Substances 0.000 claims description 22
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 22
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 21
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 claims description 21
- 235000012538 ammonium bicarbonate Nutrition 0.000 claims description 21
- 239000001099 ammonium carbonate Substances 0.000 claims description 21
- 238000000354 decomposition reaction Methods 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- MKKVKFWHNPAATH-UHFFFAOYSA-N [C].N Chemical compound [C].N MKKVKFWHNPAATH-UHFFFAOYSA-N 0.000 claims 5
- 125000004122 cyclic group Chemical group 0.000 claims 5
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000005406 washing Methods 0.000 abstract description 5
- 238000005261 decarburization Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 15
- 238000002425 crystallisation Methods 0.000 description 6
- 230000008025 crystallization Effects 0.000 description 6
- 238000010828 elution Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010792 warming Methods 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
- B01D53/34—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
- B01D53/34—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
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a carbon capturing system and a carbon capturing method by a circulating ammonia method, wherein a cooling tower connected with a flue gas channel is connected with an absorption tower, the absorption tower is connected with an inlet of a water washing tower, and a decarburization flue gas discharge channel is arranged on the water washing tower; the absorption tower is connected with a crystallizer, the crystallizer is connected with a seed crystal throwing port and an ethanol tank, and an outlet of the crystallizer is connected with an inlet of the solid-liquid separator; the solid-liquid separator is connected with the regeneration tower; the outlet of the regeneration tower is connected with the inlet of the condenser, and the liquid outlet of the condenser is connected with the liquid storage tank; the air outlet of the condenser is connected with the inlet of the gas separation and compression device, and the gas separation and compression device is connected with the liquid storage tank; the solid-liquid separator is connected with a residual liquid treatment device which is connected with an ethanol tank and a liquid storage tank; storage deviceThe liquid tank is connected with the absorption tower; the waste heat recycling device is also included. The invention adopts the circulating ammonia method carbon capturing system and the circulating ammonia method carbon capturing method, realizes the regeneration of the absorbent by utilizing the heat in the flue gas, reduces the energy consumption and improves the CO 2 Absorption rate.
Description
Technical Field
The invention relates to the technical field of flue gas decarburization, in particular to a circulating ammonia method carbon capturing system and a carbon capturing method.
Background
CCUS technology can reduce CO in global power plants at most 2 90% of emissions are considered to be the most economical way to reduce carbon emissions and slow down climate warming in the short term in the future. Wherein the chemical absorption method has great industrial application prospect, and is mainly used for absorbing CO through chemical reaction 2 Unstable reaction products are produced and the CO is recovered by reverse reaction 2 And realizes the regeneration of the absorbent, thereby achieving the purpose of capturing carbon. The ammonia water solution has the advantages of high absorption efficiency, low absorption reaction heat, low corrosiveness, low raw material price and the like, and has a plurality of added values. But there are a number of problems faced in the application process: a great deal of energy is consumed in the cooling process of the flue gas and the absorbent; the carbon capturing process is carried out at low temperature, and CO 2 The absorption rate is low; and the product can be crystallized at low temperature, which affects the stable operation of the equipment.
Disclosure of Invention
The invention aims to provide a circulating ammonia method carbon capture system, which realizes the regeneration of an absorbent by utilizing heat in flue gas, reduces energy consumption and improves CO 2 Absorption rate. Another object of the invention is to provide a carbon capturing method based on a circulating ammonia method carbon capturing system.
In order to achieve the aim, the invention provides a circulating ammonia method carbon capturing system, which comprises a cooling tower, wherein an inlet of the cooling tower is connected with a flue gas channel;
an outlet of the absorption tower is connected with an inlet of the absorption tower,
the flue gas outlet of the absorption tower is connected with the inlet of the water scrubber, and the water scrubber is provided with a decarbonized flue gas discharge channel;
the liquid outlet of the absorption tower is connected with the crystallizer, a seed crystal throwing port is arranged on the crystallizer, and the crystallizer is connected with the ethanol tank through a connecting pipe;
the outlet of the crystallizer is connected with the inlet of the solid-liquid separator, so that the separation of crystals and lean liquid is realized;
the solid crystals separated by the solid-liquid separator are conveyed to the regeneration tower through a connecting pipe, so that the decomposition and regeneration of the crystals are realized;
the outlet of the regeneration tower is connected with the inlet of the condenser, so that the condensation of water in the crystal decomposition product is realized, and the liquid outlet of the condenser is connected with the liquid storage tank;
the gas separation compression device is connected with the gas outlet of the condenser and the inlet of the gas separation compression device, so that the separation of gas in the crystal decomposition products is realized; the separated absorbent gas is connected with the liquid storage tank through a connecting pipe;
the liquid separated by the solid-liquid separator is conveyed to the residual liquid treatment device through a connecting pipe, the ethanol separated by the residual liquid treatment device is returned to the ethanol tank through the connecting pipe, and the residual liquid separated by the residual liquid treatment device is conveyed to the liquid storage tank through the connecting pipe;
the liquid outlet of the liquid storage tank is connected with the absorbent inlet of the absorption tower;
the waste heat recycling device is arranged among the cooling tower, the residual liquid treatment device, the regeneration tower, the condenser and the gas separation compression device.
Preferably, the seed crystal is ammonium bicarbonate.
Preferably, the gas separation compression device is connected with the carbon dioxide storage device through a connecting pipe, and the separated high-purity carbon dioxide gas is stored in the carbon dioxide storage device.
Preferably, the waste heat recycling device comprises a cooling tower heat exchange and a regeneration tower heat exchange, and the cooling tower heat exchange and the regeneration tower heat exchange are in heat exchange connection through a heat exchanger.
Preferably, the cooling tower heat exchange comprises a heat exchange pipe and a circulating pump, the circulating pump is arranged on the heat exchange pipe, and the cooling tower is connected with the heat exchanger through the heat exchange pipe.
Preferably, the regeneration tower heat exchange comprises a water pipe and a circulating pump, the circulating pump is arranged at one end of the water pipe, which is close to the heat exchanger, and the heat exchanger, the residual liquid treatment device, the regeneration tower, the condenser, the gas separation compression device, the circulating pump and the heat exchanger are sequentially connected through the water pipe.
A carbon capturing method based on the circulating ammonia method carbon capturing system comprises the following steps:
s1, enabling smoke to enter a cooling tower through a smoke channel, exchanging heat between high-temperature smoke in the cooling tower and water in a heat exchange pipe for exchanging heat of the cooling tower, cooling the high-temperature smoke by the water, and heating the water by the high-temperature smoke;
s2, enabling the cooled flue gas to enter an absorption tower from the bottom of the absorption tower through a connecting pipe, filling an ammonia water solution absorbent in the absorption tower, absorbing carbon dioxide in the flue gas through the ammonia water solution absorbent, sending the treated flue gas to a water scrubber through an outlet of the absorption tower through the connecting pipe, and discharging decarburized flue gas through the top end of the water scrubber;
s3, discharging the carbon-containing rich liquid in the absorption tower into a crystallizer from the bottom end of the absorption tower through a connecting pipe, adding ammonium bicarbonate seed crystals into the crystallizer, adding ethanol into the crystallizer, and forming ammonium bicarbonate crystals in the crystallizer;
s4, sending the solid-liquid mixture in the crystallizer into a solid-liquid separator through a connecting pipe to separate ammonium bicarbonate crystals from lean liquid, sending the ammonium bicarbonate crystals into a regeneration tower through the connecting pipe to regenerate, and sending the lean liquid into a residual liquid treatment device through the connecting pipe to perform separation treatment;
s5, heat exchange is carried out on high-temperature water in a heat exchange pipe in the cooling tower heat exchange with a water pipe in the regeneration tower through a heat exchanger, the water temperature in the water pipe is increased, the high-temperature water enters a residual liquid treatment device through the water pipe, the residual liquid treatment device is subjected to heat exchange and heating, separation of ethanol and ammonia water in the residual liquid treatment device is realized, the separated ethanol is sent into an ethanol tank through a connecting pipe for recycling, and ammonia water is sent into a liquid storage tank through the connecting pipe;
s6, a water pipe in the heat exchange of the regeneration tower enters the regeneration tower through a water pipe after passing through the residual liquid treatment device, and the regeneration tower is heated to decompose ammonium bicarbonate crystals in the regeneration tower;
s7, enabling the decomposed product to enter a condenser through a connecting pipe, condensing water in the decomposed product by the condenser, and sending the condensed water into a liquid storage tank through the connecting pipe; the water pipe in the heat exchange of the regeneration tower enters the condenser through the water pipe after passing through the regeneration tower, exchanges heat with the condenser, and absorbs the heat released by the condenser;
s8, enabling the decomposition products condensed by the condenser to enter a gas separation compression device through a connecting pipe, compressing in the gas separation compression device, and separating NH (NH) 3 Delivering the high-purity CO into a liquid storage tank through a connecting pipe, and separating the high-purity CO 2 Collecting in a carbon dioxide storage device through a connecting pipe; the water pipe in the heat exchange of the regeneration tower enters the gas separation compression device through the water pipe after passing through the condenser, exchanges heat with the gas separation compression device, absorbs heat released by the gas separation compression device, and returns to the heat exchanger through the circulating pump to wait for the heat exchange of the next cycle;
s9, mixing ammonia water, ammonia gas and condensed water in a liquid storage tank, and sending the mixed ammonia water absorbent into an absorbent inlet of an absorption tower through a connecting pipe to realize the recycling of the ammonia water absorbent.
The carbon capturing system and the carbon capturing method by the circulating ammonia method have the advantages and positive effects that:
1. the boiler wastewater is adopted in the cooling tower to perform heat exchange on the flue gas, the high-temperature flue gas is cooled, and the flue gas with lower temperature is favorable for reducing NH in the decarbonized flue gas 3 The ammonia escape and environmental pollution are reduced.
2. The crystallization rate and the controllability of the elution crystallization are improved by promoting the elution crystallization of the carbon-containing rich liquid in the crystallizer through the seed crystal and the ethanol.
3. Heating and decomposing the crystal product in a regeneration tower, collecting water and ammonia gas in the decomposed product in a liquid storage tank, mixing with ammonia water in a residual liquid treatment device, realizing the recycling of an ammonia water absorbent, reducing the components of the absorbent and keeping higher CO 2 Absorption capacity.
4. High purity CO produced from crystalline product 2 The carbon dioxide is collected in a carbon dioxide storage device for storage, so that the additional economic value is improved.
5. The waste heat recycling device is used for cooling high-temperature flue gas, heating the residual liquid treatment device and the regeneration tower, and utilizing heat generated by the condenser and the gas separation compression device, so that the energy consumption of the system is reduced.
The technical scheme of the invention is further described in detail through the drawings and the embodiments.
Drawings
FIG. 1 is a schematic diagram of a carbon capturing system and a carbon capturing method according to an embodiment of the present invention.
Reference numerals
1. A cooling tower; 2. an absorption tower; 3. a crystallizer; 4. a solid-liquid separator; 5. a regeneration tower; 6. a condenser; 7. a gas separation compression device; 8. a liquid storage tank; 9. a water washing tower; 10. a raffinate treatment unit; 11. an ethanol tank; 12. a circulation pump; 13. a heat exchanger; 14. a carbon dioxide storage device.
Detailed Description
The technical scheme of the invention is further described below through the attached drawings and the embodiments.
Unless defined otherwise, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The terms "first," "second," and the like, as used herein, do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that elements or items preceding the word are included in the element or item listed after the word and equivalents thereof, but does not exclude other elements or items. The terms "connected" or "connected," and the like, are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", etc. are used merely to indicate relative positional relationships, which may also be changed when the absolute position of the object to be described is changed.
Examples
FIG. 1 is a schematic diagram of a carbon capturing system and a carbon capturing method according to an embodiment of the present invention. As shown in the figure, a carbon capturing system by a circulating ammonia method,
the flue gas cooling device comprises a cooling tower 1, wherein an inlet of the cooling tower 1 is connected with a flue gas channel, high-temperature flue gas is cooled in the cooling tower 1, the problem of flue gas is reduced, and lower flue gas temperature is favorable for reducing NH in decarburized flue gas 3 The content of ammonia gas is reduced, the escape of ammonia gas is reduced, and the environmental pollution is reduced.
The outlet of the cooling tower 1 is connected with the inlet of the absorption tower 2, the absorption tower 2 is filled with an ammonia water solution absorbent, and carbon dioxide in the flue gas is absorbed by the ammonia water solution absorbent, so that the content of the carbon dioxide in the flue gas is reduced.
The flue gas outlet of the absorption tower 2 is connected with the inlet of the water scrubber 9, and the water scrubber 9 is provided with a decarbonized flue gas discharge channel. The water scrubber 9 is used for washing the decarbonization flue gas, and the decarbonization flue gas after washing is discharged through a discharge channel at the top end of the water scrubber 9.
The crystallizer 3, the liquid outlet of the absorption tower 2 is connected with the crystallizer 3, the crystallizer 3 is provided with a seed crystal throwing port, and the crystallizer 3 is connected with the ethanol tank 11 through a connecting pipe. The seed crystal is ammonium bicarbonate, and ammonia water and carbon dioxide in the crystallizer 3 generate ammonium bicarbonate crystals under the action of the seed crystal. Seed crystals are added to the crystallizer 3, which provide a ready attachment surface for supersaturated solution, facilitating the crystallization by elution. On one hand, explosive nucleation can be avoided, on the other hand, the supersaturation degree of the solution system can be consumed by the growth of the seed crystal, the thermodynamic instability of the solution system is reduced, and the solution crystallization process is easier to control.
And the outlet of the crystallizer 3 is connected with the inlet of the solid-liquid separator 4 to realize the separation of crystals and lean liquid. The solid-liquid separator 4 can be of an existing structural model as required.
And the solid crystals separated by the solid-liquid separator 4 are conveyed to the regeneration tower 5 through a connecting pipe to realize the decomposition and regeneration of the crystals.The ammonium bicarbonate crystals are heated and decomposed into CO in the regeneration tower 5 2 、NH 3 And H 2 O。
The outlet of the regeneration tower 5 is connected with the inlet of the condenser to realize the condensation of water in the crystal decomposition products, the liquid outlet of the condenser 6 is connected with the liquid storage tank 8, and the condensed water is sent into the liquid storage tank 8.
The gas separation and compression device 7, the gas outlet of the condenser 6 is connected with the inlet of the gas separation and compression device 7, so as to realize CO in the crystal decomposition product 2 、NH 3 Is separated from the (a); separated absorbent gas NH 3 Is connected with the liquid storage tank 8 through a connecting pipe. The gas separation and compression device 7 is also selected from the existing structural models as required. The gas separation and compression device 7 is connected to the carbon dioxide storage device 14 via a connection pipe, and the separated high-purity carbon dioxide gas is stored in the carbon dioxide storage device 14.
The liquid separated by the solid-liquid separator 4 is conveyed to the residual liquid treatment device 10 through a connecting pipe, and the ethanol separated by the residual liquid treatment device 10 is returned to the ethanol tank 11 through the connecting pipe, so that the recycling of the ethanol is realized. The residual liquid ammonia water separated by the residual liquid treatment device 10 is sent into the liquid storage tank 8 through a connecting pipe. The raffinate treatment apparatus 10 adopts a heating mode to separate ethanol from ammonia water.
The liquid outlet of the liquid storage tank 8 is connected with the absorbent inlet of the absorption tower 2. Ammonia water, ammonia gas and condensed water are mixed in the liquid storage tank 8, so that the recycling of the absorbent is realized, and the absorbent always keeps higher CO 2 Absorption capacity of improving CO 2 Is not limited, and the absorption rate of (a) is not limited.
The waste heat recycling device is arranged among the cooling tower 1, the residual liquid treatment device 10, the regeneration tower 5, the condenser 6 and the gas separation compression device 7. The waste heat recycling device comprises a cooling tower heat exchange and a regeneration tower heat exchange, and the cooling tower heat exchange and the regeneration tower heat exchange are in heat exchange connection through a heat exchanger 13.
The cooling tower heat exchange comprises a heat exchange pipe and a circulating pump 12, wherein the circulating pump 12 is arranged on the heat exchange pipe, and the cooling tower 1 is connected with a heat exchanger 13 through the heat exchange pipe. The heat exchange pipe exchanges heat with high-temperature flue gas in the cooling tower 1 to cool the flue gas; the circulating water in the heat exchange tube after heat exchange exchanges heat with the circulating water in the heat exchange of the regeneration tower under the action of the heat exchanger 13.
The regeneration tower heat exchange comprises a water pipe and a circulating pump 12, wherein the circulating pump 12 is arranged at one end of the water pipe, which is close to the heat exchanger 13. The heat exchanger 13, the raffinate treatment device 10, the regeneration tower 5, the condenser 6, the gas separation compression device 7, the circulating pump 12 and the heat exchanger 13 are connected through water pipes in sequence. The water in the water pipe exchanges heat with the residual liquid treatment device 10, the regeneration tower 5, the condenser 6 and the gas separation compression device 7 in sequence.
The circulating water in the waste heat recycling device can be boiler waste water.
A carbon capturing method based on the circulating ammonia method carbon capturing system comprises the following steps:
s1, flue gas enters the cooling tower 1 through a flue gas channel, high-temperature flue gas exchanges heat with water in a heat exchange tube of the cooling tower in the cooling tower 1, the water cools the high-temperature flue gas, and the high-temperature flue gas heats the water.
S2, enabling cooled flue gas to enter the absorption tower 2 from the bottom of the absorption tower 2 through a connecting pipe, filling an ammonia water solution absorbent in the absorption tower 2, absorbing carbon dioxide in the flue gas through the ammonia water solution absorbent, conveying the treated flue gas to the water scrubber 9 through an outlet of the absorption tower 2 through the connecting pipe, and discharging decarburized flue gas through the top end of the water scrubber 9.
S3, discharging the carbon-containing rich liquid in the absorption tower 2 into a crystallizer 3 from the bottom end of the absorption tower 2 through a connecting pipe, adding ammonium bicarbonate seed crystals into the crystallizer 3, adding ethanol into the crystallizer 3, and dissolving ammonia water and carbon dioxide in the crystallizer 3 on the surface of the seed crystals for crystallization to form ammonium bicarbonate crystals.
S4, sending the solid-liquid mixture in the crystallizer 3 into a solid-liquid separator 4 through a connecting pipe to separate ammonium bicarbonate crystals from lean liquid, sending the ammonium bicarbonate crystals into a regeneration tower 5 through the connecting pipe to regenerate, and sending the lean liquid into a residual liquid treatment device 10 through the connecting pipe to perform separation treatment.
S5, heat exchange is carried out between high-temperature water in the heat exchange pipe of the cooling tower and the water pipe in the heat exchange of the regeneration tower through the heat exchanger 13, the water temperature in the water pipe is increased, the high-temperature water enters the residual liquid treatment device 10 through the water pipe, the residual liquid treatment device 10 is subjected to heat exchange and heating, separation of ethanol and ammonia water in the residual liquid treatment device 10 is realized, the separated ethanol is sent into the ethanol tank 11 through a connecting pipe for recycling, and the ammonia water is sent into the liquid storage tank 8 through the connecting pipe.
S6, a water pipe in the heat exchange of the regeneration tower enters the regeneration tower 5 through the water pipe after passing through the residual liquid treatment device 10, and the regeneration tower 5 is heated to decompose ammonium bicarbonate crystals in the regeneration tower 5. The ammonium bicarbonate crystal can obtain higher decomposition rate at 70 ℃, and compared with rich liquor regeneration, the regeneration energy consumption of the product is greatly reduced.
S7, enabling the decomposed products to enter a condenser 6 through a connecting pipe, condensing water in the decomposed products by the condenser 6, and sending the condensed water into a liquid storage tank 8 through the connecting pipe. The water pipe in the heat exchange of the regeneration tower enters the condenser 6 through the water pipe after passing through the regeneration tower 5, exchanges heat with the condenser 6, and absorbs the heat emitted by the condenser 6.
S8, enabling the decomposition products condensed by the condenser 6 to enter the gas separation and compression device 7 through a connecting pipe, compressing in the gas separation and compression device 7, and separating NH 3 Is conveyed into a liquid storage tank 8 through a connecting pipe, and separated high-purity CO 2 Is collected in the carbon dioxide storage means 14 via a connecting pipe. The water pipe in the heat exchange of the regeneration tower enters the gas separation compression device 7 through the water pipe after passing through the condenser 6, exchanges heat with the gas separation compression device 7, absorbs the heat released by the gas separation compression device 7, and then returns to the heat exchanger 13 through the circulating pump 12 to wait for the heat exchange of the next cycle.
S9, mixing ammonia water, pure ammonia gas and condensed water in a liquid storage tank 8, and conveying the mixed ammonia water absorbent into an absorbent inlet of the absorption tower 2 through a connecting pipe to realize the recycling of the ammonia water absorbent.
Therefore, the invention adopts the circulating ammonia method carbon capturing system and the circulating ammonia method carbon capturing method, realizes the regeneration of the absorbent by utilizing the heat in the flue gas, reduces the energy consumption and improves the CO 2 Absorption rate.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention and not for limiting it, and although the present invention has been described in detail with reference to the preferred embodiments, it will be understood by those skilled in the art that: the technical scheme of the invention can be modified or replaced by the same, and the modified technical scheme cannot deviate from the spirit and scope of the technical scheme of the invention.
Claims (7)
1. A carbon capturing system by a circulating ammonia method is characterized in that:
the device comprises a cooling tower, wherein an inlet of the cooling tower is connected with a flue gas channel;
an outlet of the absorption tower is connected with an inlet of the absorption tower,
the flue gas outlet of the absorption tower is connected with the inlet of the water scrubber, and the water scrubber is provided with a decarbonized flue gas discharge channel;
the liquid outlet of the absorption tower is connected with the crystallizer, a seed crystal throwing port is arranged on the crystallizer, and the crystallizer is connected with the ethanol tank through a connecting pipe;
the outlet of the crystallizer is connected with the inlet of the solid-liquid separator, so that the separation of crystals and lean liquid is realized;
the solid crystals separated by the solid-liquid separator are conveyed to the regeneration tower through a connecting pipe, so that the decomposition and regeneration of the crystals are realized;
the outlet of the regeneration tower is connected with the inlet of the condenser, so that the condensation of water in the crystal decomposition product is realized, and the liquid outlet of the condenser is connected with the liquid storage tank;
the gas separation compression device is connected with the gas outlet of the condenser and the inlet of the gas separation compression device, so that the separation of gas in the crystal decomposition products is realized; the separated absorbent gas is connected with the liquid storage tank through a connecting pipe;
the liquid separated by the solid-liquid separator is conveyed to the residual liquid treatment device through a connecting pipe, the ethanol separated by the residual liquid treatment device is returned to the ethanol tank through the connecting pipe, and the residual liquid separated by the residual liquid treatment device is conveyed to the liquid storage tank through the connecting pipe;
the liquid outlet of the liquid storage tank is connected with the absorbent inlet of the absorption tower;
the waste heat recycling device is arranged among the cooling tower, the residual liquid treatment device, the regeneration tower, the condenser and the gas separation compression device.
2. The cyclic ammonia carbon capture system of claim 1, wherein: the seed crystal is ammonium bicarbonate.
3. The cyclic ammonia carbon capture system of claim 1, wherein: the gas separation compression device is connected with the carbon dioxide storage device through a connecting pipe, and the separated high-purity carbon dioxide gas is stored in the carbon dioxide storage device.
4. The cyclic ammonia carbon capture system of claim 1, wherein: the waste heat recycling device comprises a cooling tower heat exchange device and a regeneration tower heat exchange device, and the cooling tower heat exchange device and the regeneration tower heat exchange device are in heat exchange connection through a heat exchanger.
5. The cyclic ammonia carbon capture system of claim 4, wherein: the cooling tower heat exchange comprises a heat exchange pipe and a circulating pump, the circulating pump is arranged on the heat exchange pipe, and the cooling tower is connected with the heat exchanger through the heat exchange pipe.
6. The cyclic ammonia carbon capture system of claim 4, wherein: the regeneration tower heat exchange comprises a water pipe and a circulating pump, wherein the circulating pump is arranged at one end of the water pipe, which is close to the heat exchanger, and the heat exchanger, the residual liquid treatment device, the regeneration tower, the condenser, the gas separation compression device, the circulating pump and the heat exchanger are sequentially connected through water pipes.
7. A carbon capturing method based on the circulating ammonia process carbon capturing system according to any one of claims 1 to 6, characterized by comprising the steps of:
s1, enabling smoke to enter a cooling tower through a smoke channel, exchanging heat between high-temperature smoke in the cooling tower and water in a heat exchange pipe for exchanging heat of the cooling tower, cooling the high-temperature smoke by the water, and heating the water by the high-temperature smoke;
s2, enabling the cooled flue gas to enter an absorption tower from the bottom of the absorption tower through a connecting pipe, filling an ammonia water solution absorbent in the absorption tower, absorbing carbon dioxide in the flue gas through the ammonia water solution absorbent, sending the treated flue gas to a water scrubber through an outlet of the absorption tower through the connecting pipe, and discharging decarburized flue gas through the top end of the water scrubber;
s3, discharging the carbon-containing rich liquid in the absorption tower into a crystallizer from the bottom end of the absorption tower through a connecting pipe, adding ammonium bicarbonate seed crystals into the crystallizer, adding ethanol into the crystallizer, and forming ammonium bicarbonate crystals in the crystallizer;
s4, sending the solid-liquid mixture in the crystallizer into a solid-liquid separator through a connecting pipe to separate ammonium bicarbonate crystals from lean liquid, sending the ammonium bicarbonate crystals into a regeneration tower through the connecting pipe to regenerate, and sending the lean liquid into a residual liquid treatment device through the connecting pipe to perform separation treatment;
s5, heat exchange is carried out on high-temperature water in a heat exchange pipe in the cooling tower heat exchange with a water pipe in the regeneration tower through a heat exchanger, the water temperature in the water pipe is increased, the high-temperature water enters a residual liquid treatment device through the water pipe, the residual liquid treatment device is subjected to heat exchange and heating, separation of ethanol and ammonia water in the residual liquid treatment device is realized, the separated ethanol is sent into an ethanol tank through a connecting pipe for recycling, and ammonia water is sent into a liquid storage tank through the connecting pipe;
s6, a water pipe in the heat exchange of the regeneration tower enters the regeneration tower through a water pipe after passing through the residual liquid treatment device, and the regeneration tower is heated to decompose ammonium bicarbonate crystals in the regeneration tower;
s7, enabling the decomposed product to enter a condenser through a connecting pipe, condensing water in the decomposed product by the condenser, and sending the condensed water into a liquid storage tank through the connecting pipe; the water pipe in the heat exchange of the regeneration tower enters the condenser through the water pipe after passing through the regeneration tower, exchanges heat with the condenser, and absorbs the heat released by the condenser;
s8, condensing by a condenserThe decomposition products of (2) enter a gas separation and compression device through a connecting pipe, and are compressed in the gas separation and compression device, and separated NH is obtained 3 Delivering the high-purity CO into a liquid storage tank through a connecting pipe, and separating the high-purity CO 2 Collecting in a carbon dioxide storage device through a connecting pipe; the water pipe in the heat exchange of the regeneration tower enters the gas separation compression device through the water pipe after passing through the condenser, exchanges heat with the gas separation compression device, absorbs heat released by the gas separation compression device, and returns to the heat exchanger through the circulating pump to wait for the heat exchange of the next cycle;
s9, mixing ammonia water, ammonia gas and condensed water in a liquid storage tank, and sending the mixed ammonia water absorbent into an absorbent inlet of an absorption tower through a connecting pipe to realize the recycling of the ammonia water absorbent.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104107629A (en) * | 2014-08-04 | 2014-10-22 | 上海龙净环保科技工程有限公司 | System and method for capturing carbon dioxide in smoke |
| CN104180381A (en) * | 2014-08-18 | 2014-12-03 | 山东大学 | System and method for desulfurization cooling efficiency improvement and waste heat recovery |
| JP2015024374A (en) * | 2013-07-26 | 2015-02-05 | 株式会社Ihi | Carbon dioxide recovery method and recovery device |
| CN106693648A (en) * | 2016-12-08 | 2017-05-24 | 华电电力科学研究院 | Carbon dioxide capture system by employing ammonia process of strengthening crystallization and method of carbon dioxide capture system |
| CN108014603A (en) * | 2017-11-21 | 2018-05-11 | 华电电力科学研究院 | Crystallization ammonia process steam regeneration catches carbon system and method |
| CN115738634A (en) * | 2022-10-19 | 2023-03-07 | 航天环境工程有限公司 | Pneumatic ammonia desulphurization and decarbonization integrated system, method and application |
-
2023
- 2023-03-10 CN CN202310227892.8A patent/CN116785905B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2015024374A (en) * | 2013-07-26 | 2015-02-05 | 株式会社Ihi | Carbon dioxide recovery method and recovery device |
| CN104107629A (en) * | 2014-08-04 | 2014-10-22 | 上海龙净环保科技工程有限公司 | System and method for capturing carbon dioxide in smoke |
| CN104180381A (en) * | 2014-08-18 | 2014-12-03 | 山东大学 | System and method for desulfurization cooling efficiency improvement and waste heat recovery |
| CN106693648A (en) * | 2016-12-08 | 2017-05-24 | 华电电力科学研究院 | Carbon dioxide capture system by employing ammonia process of strengthening crystallization and method of carbon dioxide capture system |
| CN108014603A (en) * | 2017-11-21 | 2018-05-11 | 华电电力科学研究院 | Crystallization ammonia process steam regeneration catches carbon system and method |
| CN115738634A (en) * | 2022-10-19 | 2023-03-07 | 航天环境工程有限公司 | Pneumatic ammonia desulphurization and decarbonization integrated system, method and application |
Non-Patent Citations (1)
| Title |
|---|
| 王金英等: "《火工药剂概论》", vol. 1, 国防工业出版社, pages: 241 * |
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