CN113680179A - Flue gas purification system and comprehensive cold energy utilization process thereof - Google Patents

Flue gas purification system and comprehensive cold energy utilization process thereof Download PDF

Info

Publication number
CN113680179A
CN113680179A CN202111044328.XA CN202111044328A CN113680179A CN 113680179 A CN113680179 A CN 113680179A CN 202111044328 A CN202111044328 A CN 202111044328A CN 113680179 A CN113680179 A CN 113680179A
Authority
CN
China
Prior art keywords
flue gas
pipe
coap
liquid
heat
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN202111044328.XA
Other languages
Chinese (zh)
Other versions
CN113680179B (en
Inventor
刘练波
王焕君
郭东方
刘蓉
范金航
牛红伟
郜时旺
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Huaneng Clean Energy Research Institute
Huaneng Power International Inc
Original Assignee
Huaneng Clean Energy Research Institute
Huaneng Power International Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Huaneng Clean Energy Research Institute, Huaneng Power International Inc filed Critical Huaneng Clean Energy Research Institute
Priority to CN202111044328.XA priority Critical patent/CN113680179B/en
Publication of CN113680179A publication Critical patent/CN113680179A/en
Priority to PCT/CN2021/140607 priority patent/WO2023035493A1/en
Application granted granted Critical
Publication of CN113680179B publication Critical patent/CN113680179B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1431—Pretreatment by other processes
    • B01D53/1437—Pretreatment by adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • 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
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
    • F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2047—Hydrofluoric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
    • 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

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a flue gas purification system and a cold energy comprehensive utilization process thereof, wherein the flue gas purification system comprises a COAP system, a heat exchanger and a heat exchanger, wherein the COAP system is used for discharging flue gas after desulfurization and denitration; and the air inlet of the carbon capture system is communicated with the air outlet of the COAP system and is used for removing carbon in the flue gas discharged by the COAP system. The flue gas purification system also comprises a cold energy utilization pipeline system which is used for sequentially conveying the flue gas discharged by the COAP system to a condenser at the top of a regeneration tower and a barren solution pipe of the carbon capture system to respectively exchange heat with the discharged carbon dioxide and barren solution and then enter an absorption tower for decarburization treatment. The flue gas treated by the combined treatment of the COAP system and the carbon capture system can achieve the aims of environmental protection and double carbon, meet the requirement of flue gas evacuation, and make the cold energy utilization of the flue gas exhausted by the COAP system more sufficient.

Description

Flue gas purification system and comprehensive cold energy utilization process thereof
Technical Field
The invention relates to the technical field of energy recovery of power plants, in particular to a flue gas purification system and a comprehensive cold energy utilization process thereof.
Background
The low-temperature pollutant integrated removing technology (COAP technology for short) is a comprehensive treatment technology for flue gas pollutants, and based on the principle of flue gas low-temperature adsorption and denitration, SO is firstly removed by a desulfurization adsorption tower2And residual moisture, while also adsorbing SO3Hg, HCl, HF, VOCs and small amounts of NOx; the desulfurized and dehumidified flue gas is cooled to a temperature below zero and then enters a low-temperature denitration adsorption tower, NOx is deeply adsorbed and removed at low temperature, and two goals of 'integrated removal' and 'near zero emission' for pollutants are achieved. For example: the flue gas low-temperature adsorption denitration system and the flue gas low-temperature adsorption denitration process disclosed in the Chinese patent CN110743312A are revolutionary technologies for realizing flue gas purification of industrial kilns such as coal-fired power generation, garbage and biomass power generation, cement steel and the like.
After the flue gas is treated by the COAP technology, the flue gas treated by the low-temperature denitration adsorption tower is generally directly subjected to cold recycling and then is exhausted, but the flue gas treated by the COAP technology also contains a large amount of CO2From the viewpoint of environmental protection and dual carbon target, direct evacuation is not reasonable, and the requirement of flue gas evacuation cannot be met.
Disclosure of Invention
Therefore, the technical problem to be solved by the invention is to overcome the defect that the direct evacuation of the flue gas after the flue gas is treated by only adopting the COAP technology in the prior art can not meet the requirement of the evacuation of the flue gas, thereby providing a flue gas purification system and a comprehensive utilization process of the cooling capacity thereof for solving the problems.
A flue gas purification system comprising:
the COAP system is used for discharging flue gas after desulfurization and denitration;
and the air inlet of the carbon capture system is communicated with the air outlet of the COAP system and is used for removing carbon in the flue gas discharged by the COAP system.
The flue gas purification system also comprises a cold energy utilization pipeline system;
the carbon capture system is a CO2 chemical absorption system having a condenser and a lean liquid pipe; the cold energy utilization pipeline system comprises:
the first cold energy conveying pipeline is used for conveying the flue gas discharged by the COAP system to the condenser for cold energy utilization;
the second heat exchanger is used for exchanging heat between the flue gas discharged by the condenser and the barren liquor in the barren liquor pipe;
and the second cold energy conveying pipeline is used for conveying the flue gas subjected to heat exchange by the second heat exchanger to the air inlet of the carbon capture system.
And the outlet of the condenser is communicated with the second heat exchanger through a low-temperature flue gas communicating pipe.
The carbon capture system further comprises:
the absorption tower is provided with an air inlet, an air outlet, a liquid inlet and a liquid outlet;
the regeneration tower is provided with a liquid inlet and a liquid outlet, the bottom of the regeneration tower is provided with a reboiler, and the condenser is arranged at the top of the regeneration tower;
a liquid-rich pipe, both ends of which are respectively communicated with the liquid outlet of the absorption tower and the liquid inlet of the regeneration tower, and a liquid-rich pump is arranged on the liquid-rich pipe;
the two ends of the lean liquid pipe are respectively communicated with the liquid inlet of the absorption tower and the liquid outlet of the regeneration tower, and a lean liquid pump is arranged on the lean liquid pipe.
The carbon capture system also comprises a first heat exchanger used for heat exchange between the rich liquid pipe and the lean liquid pipe;
and the lean solution in the lean solution pipe exchanges heat with the gas in the second heat exchanger, and then exchanges heat with the rich solution in the rich solution pipe through the first heat exchanger.
The COAP system comprises a dust remover, a desulfurization adsorption tower, a refrigerator and a denitration adsorption tower which are sequentially communicated; and a gas outlet of the denitration adsorption tower is communicated with a cold air inlet of the condenser through a first cold energy conveying pipeline.
The COAP system also comprises a flue gas cooler, wherein the flue gas cooler is positioned between the dust remover and the desulfurization adsorption tower and is used for recovering heat in the flue gas; and a collecting tank for collecting condensed water in the flue gas is also arranged between the flue gas cooler and the desulfurization adsorption tower.
The flue gas is the flue gas that the boiler discharged, still include the air preheater that is located between boiler and the dust remover in the COAP system, the air preheater is used for the flue gas that the boiler discharged and gets into the heat transfer of boiler air, and the flue gas gets into in the dust remover after the heat transfer in the air preheater.
The invention discloses a flue gas purification system, which further comprises a steam heat utilization pipeline system, wherein the steam heat utilization pipeline system comprises:
the high-temperature steam conveying pipe is communicated with a regeneration gas inlet of the desulfurization adsorption tower and/or the denitration adsorption tower;
one end of the regenerated gas discharge pipe is communicated with a regenerated gas outlet of the desulfurization adsorption tower and/or the denitration adsorption tower, and the other end of the regenerated gas discharge pipe is communicated with a gas inlet of the reboiler;
one end of the steam recovery pipe is communicated with the gas outlet of the reboiler.
And the steam in the steam recovery pipe exchanges heat with the flue gas in the second cold energy conveying pipeline and then is discharged.
The process for comprehensively utilizing the cold energy by adopting the flue gas purification system comprises the following steps:
the low-temperature flue gas discharged by the COAP system firstly enters a condenser of the carbon capture system to cool the discharged CO2 gas, then exchanges heat with lean solution in the carbon capture system, and finally enters the carbon capture system to remove CO2 gas in the flue gas.
The invention also discloses a process for comprehensively utilizing heat by adopting the flue gas purification system, which comprises the following steps:
high-temperature steam of a power plant steam turbine as regeneration gas firstly enters a desulfurization adsorption tower and/or a denitration adsorption tower for regeneration of an adsorbent, the temperature of the steam passing through the desulfurization adsorption tower and/or the denitration adsorption tower is reduced to 200-plus-300 ℃, then the steam enters a reboiler for heating chemical adsorption liquid in the regeneration tower and then is reduced to 100-plus-150 ℃, and then the steam exchanges heat with low-temperature flue gas entering a carbon capture system and is cooled again, and then the steam enters a subsequent steam utilization system.
The subsequent steam utilization system comprises a power plant heater or/and a deaerator.
The technical scheme of the invention has the following advantages:
1. according to the flue gas purification system provided by the invention, the COAP system and the carbon capture system are used in a combined manner, so that SOx, NOx, Hg, HCl, HF, VOCs and the like in the flue gas of a power plant can be removed by using the COAP process; meanwhile, carbon in the flue gas can be removed by combining the carbon capture system, and the flue gas treated by the COAP system and the carbon capture system can achieve the aims of environmental protection and double carbon, so that the requirement of flue gas evacuation is met.
2. The flue gas purification system further increases a cold energy utilization pipeline system, and the cold energy utilization pipeline system is used for gradually utilizing the cold energy of the low-temperature flue gas generated by the COAP system, so that the cold energy recovery is effectively realized; specifically, the low-temperature flue gas generated by the COAP system is firstly subjected to cold energy utilization in a condenser of the carbon capture system, then is subjected to heat exchange with hot barren liquor in the carbon capture system, so that the cold energy is secondarily utilized, and finally the flue gas subjected to cold energy utilization is introduced into the carbon capture system to be evacuated after carbon dioxide removal; by the method, refrigeration equipment does not need to be additionally arranged in the carbon capture system, and meanwhile, the cold energy is more fully utilized.
3. The flue gas purification system provided by the invention is further additionally provided with a steam heat utilization pipeline system, so that the flue gas purification system not only can be applied to large coal-fired power plant boilers, but also can be used for removing pollutants in various industrial tail gases such as waste incineration, coke oven furnaces and the like, and particularly can improve the competitiveness of a thermal power plant when being applied to a molded coal-fired power plant boiler, and can achieve the triple targets of zero emission of pollutants, carbon dioxide emission reduction and comprehensive energy utilization; the steam heat utilization pipeline system can adopt high-quality steam from a steam turbine of a power plant, and realize gradual utilization along with the reduction of temperature in a COAP process and a carbon capture process, so that the utilization rate of heat is improved; according to measurement and calculation, under the condition of realizing near zero emission index, the direct operation cost of the invention is only 0.015-0.02 yuan/kWh, and the invention can be completely covered by conventional ultralow emission desulfurization and denitration subsidy electricity price.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic diagram of the overall structure of a flue gas purification system according to the present invention;
fig. 2 is a structural view of a carbon capture system having a refrigeration capacity utilization piping system according to the present invention at a location.
Description of reference numerals:
1-COAP system, 2-carbon capture system, 3-cold energy utilization pipeline system, 4-steam heat utilization pipeline system;
11-a dust remover, 12-a desulfurization adsorption tower, 13-a refrigerator, 14-a denitration adsorption tower, 15-a flue gas cooler, 16-a collection tank and 17-an air preheater;
21-absorption tower, 22-regeneration tower, 23-rich liquor pipe, 24-rich liquor pump, 25-lean liquor pipe, 26-lean liquor pump, 27-reboiler, 28-condenser, 29-first heat exchanger;
31-a first cold energy conveying pipeline, 32-a second heat exchanger, 33-a second cold energy conveying pipeline and 34-a low-temperature flue gas communicating pipe;
41-high temperature steam conveying pipe, 42-regeneration gas discharge pipe, 43-steam recovery pipe and 44-third heat exchanger.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "front", "rear", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, the technical features involved in the different embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
Example 1
A flue gas purification system comprises a COAP system 1 and a carbon capture system 2, wherein an air inlet of the carbon capture system is communicated with an air outlet of the COAP system 1. The COAP system 1 is used for discharging flue gas after desulfurization and denitration, and the carbon capture system 2 is used for removing carbon in the flue gas discharged by the COAP system 1.
The invention adopts the combined use of the COAP system and the carbon trapping system, and not only can the SOx, NOx, Hg, HCl, HF, VOCs and the like in the flue gas of the power plant be treated and removed by using the COAP process; meanwhile, carbon in the flue gas can be removed by combining the carbon capture system, and the flue gas treated by the COAP system and the carbon capture system can achieve the aims of environmental protection and double carbon, so that the requirement of flue gas evacuation is met.
The COAP system 1 in this embodiment may be a conventional COAP system, or may be a COAP system after structure optimization. The carbon capture system 2 may be one of several categories, chemical absorption, physical adsorption, membrane separation, cryogenic separation, and the like. The flue gas emptying requirement of the invention can be met as long as the carbon of the flue gas exhausted by the COAP system can be removed.
Example 2
This embodiment has further optimized the structure of a flue gas purification system on the basis of embodiment 1, and this carbon capture system 2 is CO2 chemical absorption system in this embodiment, has increased simultaneously and has set up cold volume and utilized pipe-line system 3, effectively carries out reasonable application to the cold volume in the low temperature flue gas that COAP system 1 discharged, as shown in FIG. 2, specifically as follows:
the carbon capture system 2 includes an absorption tower 21, a regeneration tower 22, a rich liquid pipe 23, a rich liquid pump 24, a lean liquid pipe 25, a lean liquid pump 26, a reboiler 27, and a condenser 28. Wherein, the absorption tower 21 is provided with an air inlet, an air outlet, a liquid inlet and a liquid outlet, and the regeneration tower 22 is provided with a liquid inlet, a liquid outlet and an air outlet; the bottom of the regeneration tower 22 is provided with a reboiler 27, and the top exhaust port is provided with a condenser 28; two ends of the rich liquid pipe 23 are respectively communicated with a liquid outlet of the absorption tower 21 and a liquid inlet of the regeneration tower 22, and a rich liquid pump 24 is arranged on the rich liquid pipe; the lean liquid pipe 25 has both ends respectively connected to the liquid inlet of the absorption tower 21 and the liquid outlet of the regeneration tower 22, and is provided with a lean liquid pump 26, as shown in fig. 2.
As shown in fig. 1, the COAP system 1 includes a dust collector 11, a desulfurization adsorption tower 12, a refrigerator 13, and a denitration adsorption tower 14, which are connected in sequence.
The cold energy utilization pipeline system 3 comprises a first cold energy conveying pipeline 31, a second heat exchanger 32, a low-temperature flue gas communicating pipe 34 and a second cold energy conveying pipeline 33; wherein, two ends of the first cold conveying pipeline 31 are respectively communicated with the gas outlet of the denitration adsorption tower 14 and the cold air inlet of the condenser 28, and are used for conveying the flue gas discharged by the COAP system 1 to the condenser 28 for cold utilization. The second heat exchanger 32 comprises a flue gas line and a lean liquid line, respectively, for exchanging heat between the flue gas discharged from the condenser 28 and the lean liquid in the lean liquid pipe 25. The low-temperature flue gas communicating pipe 34 is respectively communicated with the cold air outlet of the condenser 28 and the flue gas inlet of the second heat exchanger 32, and is used for conveying the low-temperature flue gas in the condenser 28 to the second heat exchanger 32 for heat exchange. The second cold energy conveying pipeline 33 is respectively communicated with a flue gas outlet in the second heat exchanger 32 and an air inlet of the absorption tower 21 in the carbon capture system 2, and is used for conveying the flue gas subjected to further temperature increase after heat exchange by the second heat exchanger 32 to the carbon capture system 2 for decarbonization.
Through the optimization of the structure, the cold quantity of the low-temperature flue gas discharged from the COAP process can be fully utilized.
For better utilization of the heat in the lean liquor, the carbon capture system 2 further comprises a first heat exchanger 29 for heat exchange between the rich liquor pipe 23 and the lean liquor pipe 25, as shown in fig. 2; the lean solution in the lean solution pipe 25 exchanges heat with the flue gas in the second heat exchanger 32, and then exchanges heat with the rich solution in the rich solution pipe 23 through the first heat exchanger 29.
Because the temperature of the flue gas entering the COAP system 1 is high, in order to avoid energy waste, the COAP system 1 further comprises a flue gas cooler 15, the flue gas cooler 15 is located between the dust remover 11 and the desulfurization adsorption tower 12, and is used for cooling the flue gas and recovering heat in the flue gas, and the recovered heat can be used for other applications. A collection tank 16 for collecting condensed water in the flue gas is further arranged between the flue gas cooler 15 and the desulfurization adsorption tower 12, as shown in fig. 1. When the flue gas is the flue gas discharged by the boiler, the COAP system 1 further comprises an air preheater 17 located between the boiler and the dust remover 11, the air preheater 17 is used for exchanging heat between the flue gas discharged by the boiler and air entering the boiler, and the flue gas enters the dust remover 11 after exchanging heat in the air preheater 17.
Example 3
The structure of a gas cleaning system has further been optimized on embodiment 2 basis to this embodiment, has still increased in this embodiment and has set up steam heat utilization pipe-line system 4, and it can utilize the steam of the different qualities of power plant step by step, improves energy utilization, specifically as follows:
the steam heat utilization piping system 4 includes a high-temperature steam delivery pipe 41, a regeneration gas discharge pipe 42, a steam recovery pipe 43, and a third heat exchanger 44. Wherein, the high-temperature steam conveying pipe 41 is communicated with a regeneration gas inlet of the desulfurization adsorption tower 12 and/or the denitration adsorption tower 14; the high-temperature steam which is discharged by a power plant steam turbine and reaches the temperature of 300-350 ℃ is used as the regeneration gas, and the temperature of the regeneration gas which is used as the regeneration gas and is subjected to adsorbent regeneration in the desulfurization adsorption tower 12 and/or the denitration adsorption tower 14 is reduced to 200-300 ℃. One end of the regenerated gas discharge pipe 42 is communicated with a regenerated gas outlet of the desulfurization adsorption tower 12 and/or the denitration adsorption tower 14, and the other end is communicated with a gas inlet of the reboiler 27; and is used for conveying the regeneration gas after the adsorbent is regenerated to the reboiler 27 to heat the barren solution in the regeneration tower 22 so as to promote the removal of carbon dioxide in the barren solution, and the temperature of the steam discharged from the reboiler 27 after the barren solution is heated is further reduced to 100-150 ℃ and is about 120 ℃. The steam recovery pipe 43 is used for conveying the high-temperature gas output by the reboiler 27 to the rear end of the cold energy utilization pipeline system 3 to continuously exchange heat with the flue gas conveyed into the carbon capture system 2; specifically, the steam in the steam recovery pipe 43 and the flue gas in the second cold energy conveying pipeline 33 are discharged after heat exchange through the third heat exchanger 44, and the temperature of the steam after heat exchange can still reach about 80-90 ℃. In order to better utilize the heat of the part of the steam, the discharged steam can be also conveyed to a subsequent steam utilization system for utilization, such as: a power plant heater or/and a deaerator.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications therefrom are within the scope of the invention.

Claims (11)

1. A flue gas purification system, comprising:
the COAP system (1) is used for discharging flue gas after desulfurization and denitration;
and the air inlet of the carbon capture system (2) is communicated with the air outlet of the COAP system (1) and is used for removing carbon in the flue gas discharged by the COAP system (1).
2. A flue gas purification system according to claim 1, further comprising a refrigeration utilization pipe system (3);
the carbon capture system (2) is CO with a condenser (28) and a lean liquid pipe (25)2A chemical absorption system; the cold energy utilization piping system (3) includes:
the first cold conveying pipeline (31) is used for conveying the flue gas discharged by the COAP system (1) to the condenser (28) for cold utilization;
the second heat exchanger (32) is used for exchanging heat between the flue gas discharged by the condenser (28) and the barren liquor in the barren liquor pipe (25);
and the second cold energy conveying pipeline (33) is used for conveying the flue gas subjected to heat exchange through the second heat exchanger (32) to the air inlet of the carbon capture system (2).
3. A flue gas cleaning system according to claim 2, wherein the condenser (28) communicates with the second heat exchanger (32) via a low temperature flue gas communication pipe (34).
4. A flue gas cleaning system according to claim 2 or 3, wherein the carbon capture system (2) further comprises:
an absorption tower (21) having an air inlet, an air outlet, a liquid inlet and a liquid outlet;
a regeneration column (22) having a liquid inlet and a liquid outlet, the bottom of which is provided with a reboiler (27), the condenser (28) being provided at a top position thereof;
a liquid-rich pipe (23), both ends of which are respectively communicated with the liquid outlet of the absorption tower (21) and the liquid inlet of the regeneration tower (22), and a liquid-rich pump (24) is arranged on the liquid-rich pipe;
and two ends of the lean liquid pipe (25) are respectively communicated with a liquid inlet of the absorption tower (21) and a liquid outlet of the regeneration tower (22), and a lean liquid pump (26) is arranged on the lean liquid pipe (25).
5. A flue gas cleaning system according to claim 4, characterized in that the carbon capture system (2) further comprises a first heat exchanger (29) for heat exchange between the rich liquor pipe (23) and the lean liquor pipe (25);
the lean liquid in the lean liquid pipe (25) exchanges heat with the gas in the second heat exchanger, and then exchanges heat with the rich liquid in the rich liquid pipe (23) through the first heat exchanger (29).
6. A flue gas purification system according to claim 4, wherein the COAP system (1) comprises a dust collector (11), a desulfurization adsorption tower (12), a refrigerator (13) and a denitration adsorption tower (14) which are communicated in sequence; and a gas outlet of the denitration adsorption tower (14) is communicated with a cold gas inlet of the condenser (28) through a first cold energy conveying pipeline (31).
7. A flue gas cleaning system according to claim 6, wherein the COAP system (1) further comprises a flue gas cooler (15), the flue gas cooler (15) is located between the dust separator (11) and the desulfurization adsorption tower (12) for recovering heat in the flue gas; and a collecting tank (16) for collecting condensed water in the flue gas is also arranged between the flue gas cooler (15) and the desulfurization adsorption tower (12).
8. A flue gas purification system according to claim 6, wherein the flue gas is flue gas discharged from a boiler, the COAP system (1) further comprises an air preheater (17) located between the boiler and the dust remover (11), the air preheater (17) is used for exchanging heat between the flue gas discharged from the boiler and air entering the boiler, and the flue gas enters the dust remover (11) after exchanging heat in the air preheater (17).
9. A flue gas cleaning system according to any of claims 6-8, further comprising a steam heat utilization pipe system (4), said steam heat utilization pipe system (4) comprising:
the high-temperature steam conveying pipe (41) is communicated with a regeneration gas inlet of the desulfurization adsorption tower (12) and/or the denitration adsorption tower (14);
a regenerated gas discharge pipe (42), one end of which is communicated with a regenerated gas outlet of the desulfurization adsorption tower (12) and/or the denitration adsorption tower (14), and the other end of which is communicated with a gas inlet of the reboiler (27);
and one end of the steam recovery pipe (43) is communicated with the air outlet of the reboiler (27).
10. A flue gas purification system according to claim 9, wherein the steam in the steam recovery pipe (43) exchanges heat with the flue gas in the second cold energy delivery pipe (33) and is discharged after the heat exchange by the third heat exchanger (44).
11. A process for the integrated utilization of cold energy by means of a flue gas purification system according to any one of claims 2 to 10, characterized in that it comprises:
the low-temperature flue gas discharged by the COAP system (1) firstly enters a condenser (28) of the carbon capture system (2) to remove the discharged CO2Cooling the gas, then exchanging heat with barren solution in the carbon capture system (2), and finally entering the carbon capture system (2) for CO in the flue gas2And (4) removing the gas.
CN202111044328.XA 2021-09-07 2021-09-07 Flue gas purification system and cold energy comprehensive utilization process thereof Active CN113680179B (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN202111044328.XA CN113680179B (en) 2021-09-07 2021-09-07 Flue gas purification system and cold energy comprehensive utilization process thereof
PCT/CN2021/140607 WO2023035493A1 (en) 2021-09-07 2021-12-22 Flue gas purification system and cold energy comprehensive utilization process therefor

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111044328.XA CN113680179B (en) 2021-09-07 2021-09-07 Flue gas purification system and cold energy comprehensive utilization process thereof

Publications (2)

Publication Number Publication Date
CN113680179A true CN113680179A (en) 2021-11-23
CN113680179B CN113680179B (en) 2023-06-23

Family

ID=78585751

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111044328.XA Active CN113680179B (en) 2021-09-07 2021-09-07 Flue gas purification system and cold energy comprehensive utilization process thereof

Country Status (2)

Country Link
CN (1) CN113680179B (en)
WO (1) WO2023035493A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023035493A1 (en) * 2021-09-07 2023-03-16 中国华能集团清洁能源技术研究院有限公司 Flue gas purification system and cold energy comprehensive utilization process therefor
WO2023035492A1 (en) * 2021-09-07 2023-03-16 中国华能集团清洁能源技术研究院有限公司 Flue gas purification system capable of comprehensively utilizing heat, and process using same

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2371238C2 (en) * 2007-12-19 2009-10-27 Государственное образовательное учреждение высшего профессионального образования "Курский государственный технический университет" Complex method and device for smoke gas cleaning with recovery of heat, harmful impurities and carbon dioxide
CN101716458A (en) * 2010-01-14 2010-06-02 中电投远达环保工程有限公司 System for trapping carbon dioxide in flue gas of coal-fired power plant and corresponding treatment method
CN110180317A (en) * 2019-06-18 2019-08-30 中国华能集团有限公司 System and method that is a kind of while removing carbon dioxide in flue gas and sulfur dioxide
GB2595553B (en) * 2019-10-29 2024-02-07 Huaneng Clean Energy Res Inst Low-temperature adsorption flue gas denitration system and process
CN110743312A (en) * 2019-10-29 2020-02-04 中国华能集团有限公司 Flue gas low-temperature adsorption denitration system and process
CN112774401A (en) * 2021-01-05 2021-05-11 中国神华能源股份有限公司国华电力分公司 Novel flue gas CO2Regeneration process of trapping system
CN113680179B (en) * 2021-09-07 2023-06-23 中国华能集团清洁能源技术研究院有限公司 Flue gas purification system and cold energy comprehensive utilization process thereof

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023035493A1 (en) * 2021-09-07 2023-03-16 中国华能集团清洁能源技术研究院有限公司 Flue gas purification system and cold energy comprehensive utilization process therefor
WO2023035492A1 (en) * 2021-09-07 2023-03-16 中国华能集团清洁能源技术研究院有限公司 Flue gas purification system capable of comprehensively utilizing heat, and process using same

Also Published As

Publication number Publication date
CN113680179B (en) 2023-06-23
WO2023035493A1 (en) 2023-03-16

Similar Documents

Publication Publication Date Title
CN113680179B (en) Flue gas purification system and cold energy comprehensive utilization process thereof
CN104154548B (en) A kind of technique of gas fired-boiler exhaust heat-energy recovery and purification of nitrogen oxides
CN114768488A (en) Coal-fired unit flue gas carbon dioxide entrapment system
CN111841066A (en) System and method for removing acid gas in flue gas
JP5573354B2 (en) Organic solvent recovery system
CN201643947U (en) Zero-discharge gas drying device
CN109794137A (en) A kind of method and system of adsorption cleaning and enriching and recovering flue gas nitrogen oxide
CN106422647B (en) Low liquefaction temperature organic waste gas recovery device
CN113813744A (en) Promote CO in coal fired boiler flue gas2System and method for capture economics
CN106310881A (en) Regenerable cyclic absorption flue gas desulfurization technology
CN113663466B (en) Flue gas purification system and process for comprehensively utilizing heat
CN108854423B (en) Flue gas waste heat driven desulfurization, denitration and carbon capture coupled flue gas purification system and flue gas treatment method
CN218077173U (en) Coke oven flue gas carbon dioxide capture system
CN217829547U (en) Low-cost organic amine method flue gas carbon dioxide entrapment system
CN112774401A (en) Novel flue gas CO2Regeneration process of trapping system
WO2017126149A1 (en) Carbon dioxide separation/recovery device, combustion system using same, thermal power generation system using same, and method for separating and recovering carbon dioxide
CN111298604A (en) System and method for capturing carbon dioxide in flue gas
CN217829546U (en) Chemical method flue gas carbon dioxide entrapment system
CN217410284U (en) Novel chemical absorption method flue gas CO2 entrapment system
CN206295762U (en) A kind of low condensing temperature air separator of oxygenerator
CN114272735B (en) Flue gas waste heat utilization and carbon capture integrated system
CN115253608A (en) Flue gas carbon capture system and method for coal-fired power generating unit
CN115608133A (en) Flue gas carbon capture system and method for capturing carbon in flue gas
CN115445377A (en) Carbon dioxide capture system for flue gas of thermal power generating unit
CN115006963A (en) System and process for recycling cryogenic solvent from waste gas in pharmaceutical industry

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant