CN117482739A - Flue gas cooperative treatment system and flue gas cooperative treatment method - Google Patents

Flue gas cooperative treatment system and flue gas cooperative treatment method Download PDF

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Publication number
CN117482739A
CN117482739A CN202311401637.7A CN202311401637A CN117482739A CN 117482739 A CN117482739 A CN 117482739A CN 202311401637 A CN202311401637 A CN 202311401637A CN 117482739 A CN117482739 A CN 117482739A
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CN
China
Prior art keywords
slurry
flue gas
cyclone separator
tank
capturing tower
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Pending
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CN202311401637.7A
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Chinese (zh)
Inventor
常林
余学海
韩涛
张帅
刘毅
赵瑞
史晓宏
徐冬
冯蕾
冯白阳
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Guoneng Guohua Beijing Electric Power Research Institute Co ltd
National Energy Group New Energy Technology Research Institute Co Ltd
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Guoneng Guohua Beijing Electric Power Research Institute Co ltd
National Energy Group New Energy Technology Research Institute Co Ltd
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Priority to CN202311401637.7A priority Critical patent/CN117482739A/en
Publication of CN117482739A publication Critical patent/CN117482739A/en
Pending legal-status Critical Current

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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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/02—Settling tanks with single outlets for the separated liquid
    • 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
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen 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
    • B01D53/46—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
    • B01D53/76—Gas phase processes, e.g. by using aerosols
    • 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
    • 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
    • B01D2257/402—Dinitrogen oxide
    • 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
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • 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

Abstract

The invention relates to the technical field of flue gas purification and discloses a flue gas cooperative treatment system and a flue gas cooperative treatment method, wherein the system comprises a capturing tower, a flocculation basin, a cyclone separator and a regeneration tank which are sequentially communicated along the trend of materials; the capturing tower is provided with a flue gas inlet, an exhaust port and a slurry inlet, a spray pipe is arranged above the inside of the capturing tower, a slurry tank is arranged below the inside of the capturing tower, and the slurry inlet is used for injecting slurry into the slurry tank; the capturingThe tower is also provided with a circulating pump, and the circulating pump is used for circularly conveying the slurry in the slurry tank to the spray pipe for circular spraying; the inside of the capturing tower is provided with a heater, the bottom of the capturing tower is provided with a plurality of aeration openings, the aeration openings are used for introducing ozone into the capturing tower, and the ozone and the flue gas react with the slurry in the capturing tower; the flue gas contains NO x 、SO 2 And CO 2 。

Description

Flue gas cooperative treatment system and flue gas cooperative treatment method
Technical Field
The invention relates to the technical field of flue gas purification, in particular to a flue gas cooperative treatment system and a flue gas cooperative treatment method.
Background
At present, the smoke NO x 、SO 2 CO 2 Such contaminant treatment techniques are mostly independent treatment processes for a single contaminant. In SO form 2 The method mainly comprises wet desulfurization, dry desulfurization and semi-dry desulfurization, wherein limestone-gypsum wet desulfurization using limestone as desulfurizing agent is widely used, and market share is relatively high, and the method comprises the steps of pulping by means of quicklime, circulating spraying in a desulfurizing tower, carrying out forced oxidation process along with tower bottom slurry during spraying circulation, and purifying oxidation productsAnd (5) gypsum production is carried out. NO (NO) x The treatment of (2) adopts an ammonia method selective catalytic reduction method, and uses a denitration catalyst to treat NO x The method requires the catalyst to react in a proper temperature range, and simultaneously requires the catalyst to have the characteristics of higher selectivity, high anti-middle toxicity, high mechanical wear resistance and the like, and the cost of the actual operation process is higher. In addition, for high concentration CO such as electric power, steel, cement and the like 2 For emission industry, reducing CO in enterprise production process 2 The emission is urgent, and the chemical absorption method based on only organic amines such as MEA is suitable for large-scale flue gas CO 2 The method has the disadvantages of high cost, complex system, low energy consumption and economy of regeneration desorption and the like, which restricts the wide-range application of the technology across industries. With further expansion of the carbon capture scale, the high energy consumption of the carbon capture system reduces the economy of the unit and the problem caused by deep coupling operation with the unit is not ignored. There is currently NO known method for NO-containing x 、SO 2 CO 2 Is a smoke co-processing system and a co-processing method.
Disclosure of Invention
The invention aims to solve the problem of independent dispersion of a flue gas removal technology in the prior art, and provides a flue gas cooperative treatment system and a flue gas cooperative treatment method, wherein the system has high overall integration level and can realize NO in flue gas x 、SO 2 CO 2 And to obtain a high quality gypsum material and to recover high purity CO 2 。
In order to achieve the above object, according to one aspect of the present invention, there is provided a flue gas co-processing system, which includes a capturing tower, a flocculation basin, a cyclone separator and a regeneration tank which are sequentially communicated along a material trend; the capturing tower is provided with a flue gas inlet, an exhaust port and a slurry inlet, a spray pipe is arranged above the inside of the capturing tower, a slurry tank is arranged below the inside of the capturing tower, and the slurry inlet is used for injecting slurry into the slurry tank; the capturing tower is also provided with a circulating pump, and the circulating pump is used for circularly conveying the slurry in the slurry tank to the spray pipe for circular spraying; the inside of the capturing tower is provided with a heating partThe bottom of the capturing tower is provided with a plurality of aeration openings, the aeration openings are used for introducing ozone into the capturing tower, and the ozone and the flue gas react with the slurry in the capturing tower; the flue gas contains NO x 、SO 2 And CO 2 。
Preferably, the number of the aeration openings is 3-6.
Preferably, the aeration openings are arranged at the bottom of the capturing tower according to concentric circles.
Preferably, the bottom of the flocculation basin is arranged obliquely with respect to the horizontal plane.
Preferably, the included angle theta between the bottom of the flocculation dropping pool and the horizontal plane is 5-10 degrees.
Preferably, the cyclone separator comprises a first cyclone separator, a second cyclone separator and a third cyclone separator.
Preferably, the bottom discharge port of the first cyclone separator is connected with the feed port of the second cyclone separator, and the bottom discharge port of the second cyclone separator is connected with the feed port of the third cyclone separator.
Preferably, the top discharge port of the first cyclone separator, the top discharge port of the second cyclone separator and the top discharge port of the third cyclone separator are respectively connected with the spray pipe.
Preferably, the system further comprises a compressor connected to the top of the regeneration tank, the compressor being for compressing CO from the regeneration tank 2 。
Preferably, the system further comprises a shower head for spraying the gypsum suspension from the regeneration tank onto the negative pressure transfer belt.
The second aspect of the present invention provides a flue gas co-processing method, which is implemented in the flue gas co-processing system, and comprises the following steps:
(1) Injecting slurry into the slurry tank from the slurry inlet, and circularly conveying the slurry in the slurry tank to the spray pipe for circular spraying through a circulating pump;
(2) Introducing flue gas into the capturing tower from the flue gas inlet, introducing ozone into the capturing tower from the aeration port, and reacting the ozone, the flue gas and the slurry in the capturing tower to obtain a reaction material; the inside of the capturing tower is provided with a heater, and the flue gas contains NO x 、SO 2 And CO 2 ；
(3) The reaction materials are conveyed into a flocculation dropping tank for sedimentation, then conveyed into a cyclone separator for cyclone separation, and then conveyed into a regeneration tank for reaction, thus obtaining CO 2 And gypsum suspension; the regeneration tank is filled with a sulfuric acid solution.
Preferably, in step (2), the temperature of the reaction is 40-70 ℃.
Preferably, in step (3), the concentration of the sulfuric acid solution is 20-40wt.%.
Preferably, in step (3), the reaction conditions include: the temperature is 30-40deg.C, and the time is 15-30min.
Preferably, the slurry is Ca (OH) 2 A suspension.
Preferably, the Ca (OH) 2 The suspension had a concentration of 6-8wt.%.
Preferably, the Ca (OH) 2 The volume ratio of the suspension to the flue gas to the ozone is 1: (23.33-23.34): (0.51-0.52).
Through the technical scheme, the bottom of the capturing tower is provided with a plurality of aeration openings, ozone is introduced into the capturing tower from the aeration openings, and NO contained in the flue gas x 、SO 2 CO 2 Can react with the slurry and ozone in series to realize NO in the flue gas x 、SO 2 CO 2 And obtaining high quality gypsum material and CO in a regeneration tank 2 ，CO 2 High purity CO can be obtained after drying 2 。
Drawings
FIG. 1 is a schematic diagram of a flue gas co-processing system according to the present invention.
Description of the reference numerals
1. A capture column; 11. a shower pipe; 12. an aeration port; 13. a slurry tank; 14. a flue gas inlet; 15. an exhaust port; 16. a slurry inlet; 2. a flocculation dropping pool; 3. a cyclone separator; 31. a first cyclone separator; 32. a second cyclone separator; 33. a third cyclone separator; 4. a regeneration tank; 5. a compressor; 6. a spray header.
Detailed Description
The following describes specific embodiments of the present invention in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In addition, if there is a description of "first", "second", etc. in the embodiments of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In addition, the technical solutions provided in the embodiments of the present invention may be combined with each other, but it is necessary to use those skilled in the art as a basis, and when the technical solutions are contradictory or cannot be implemented, it should be considered that the combination of the technical solutions does not exist and is not within the scope of protection claimed in the present invention.
In one aspect, the invention provides a flue gas co-processing system, as shown in fig. 1, which comprises a capturing tower 1, a flocculation basin 2, a cyclone separator 3 and a regeneration tank 4 which are sequentially communicated along the material trend; the capturing tower 1 is provided with a flue gas inlet 14, an exhaust port 15 and a slurry inlet 16, a spray pipe 11 is arranged above the inside of the capturing tower 1, a slurry tank 13 is arranged below the inside of the capturing tower 1, and the slurry inlet 16 is used for injecting slurry into the slurry tank 13; the capturing tower 1 is also provided with a circulating pump, and the circulating pump is used for circularly conveying the slurry in the slurry tank 13 into the spray pipe 11 for circular spraying; the bottom of the capturing tower 1 is provided with a plurality of aeration openings 12, the aeration openings 12 are used for introducing ozone into the capturing tower 1, and the ozone and the flue gas react with the slurry in the capturing tower 1.
In the system according to the invention, the volume of the vat 13 is 8-15L. Specifically, the volume of the slurry tank 13 may be 8L, 10L, 12L or 15L.
In the specific embodiment of the invention, the capturing tower 1 is provided with a slurry inlet 16 on the side wall higher than the height of the slurry tank 13, so that the slurry is smoothly injected into the slurry tank 13.
In a preferred embodiment of the present invention, in order to uniformly disperse the slurry in the slurry tank 13, a stirrer is provided under the inside of the slurry tank 13, and the stirring speed of the stirrer is 40 to 60rpm, preferably 45 to 55rpm. Specifically, the stirring speed of the stirrer may be 45rpm, 50rpm or 55rpm.
In a specific embodiment of the present invention, the capturing tower 1 is provided with a flue gas inlet 14 on a side wall lower than the height of the slurry tank 13, and flue gas is introduced into the capturing tower 1 from the flue gas inlet 14, so that the flue gas is convenient to diffuse upwards in the capturing tower 1, and the flue gas reacts with the slurry sprayed downwards by the spray pipe 11 in the process of diffusing upwards.
In a preferred embodiment of the present invention, a plurality of aeration openings 12 are provided at the bottom of the capturing tower 1, ozone is introduced into the capturing tower 1 from the aeration openings 12, and the reaction between the flue gas and the slurry is promoted.
In the system of the invention, the exhaust port 15 is arranged at the top of the capturing tower 1, and the exhaust port 15 is used for exhausting a small amount of unreacted NO in the flue gas x 、SO 2 、CO 2 Other components contained in the flue gasDividing into two parts.
In the system according to the invention, the pressure in the capturing column 1 is normal pressure. In the system according to the invention, the number of aeration openings 12 is 3-6. Specifically, the number of the aeration openings 12 may be 3, 4, 5 or 6.
In a preferred embodiment of the present invention, a plurality of the aeration openings 12 are arranged in concentric circles at the bottom of the capturing tower 1 in order to uniformly disperse ozone in the capturing tower 1.
In the system according to the invention, a heater is arranged inside the capturing tower 1 for heating the slurry to promote the reaction of the flue gas with the slurry. In a preferred case, the heating temperature of the heater is 40-70 ℃, and in particular, the heating temperature of the heater may be 40 ℃, 50 ℃, 60 ℃ or 70 ℃.
In the preferred case of the invention, the outlet of the chest 13 is connected to the flocculation basin 2 by means of a pipe, and a first transfer pump is arranged on the pipe. In the system of the invention, the reaction materials are obtained after the slurry reacts with ozone and flue gas in the capturing tower 1, the reaction materials are accumulated in the slurry tank 13, and the reaction materials in the slurry tank 13 are conveyed to the flocculation dropping tank 2 through a pipeline under the action of the first conveying pump through the outlet of the slurry tank 13 for sedimentation.
In the system of the invention, when a proper amount of flue gas, ozone and slurry are introduced into the capturing tower 1, the flue gas, ozone and slurry react to obtain reaction materials, the reaction materials are gathered in the slurry tank 13 and are mixed with unreacted slurry to obtain liquid slurry, the reaction materials are gradually increased, the unreacted slurry is reduced, and the density of the liquid slurry is gradually changed along with the progress of the reaction in the capturing tower 1, therefore, in the system of the invention, a density monitor is also arranged at the outlet of the slurry tank 13 and is used for monitoring the density of the liquid slurry in the slurry tank 13, and when the density of the liquid slurry in the slurry tank 13 reaches 1.05-1.1g/cm 3 After that, the representative materials are fully reacted, and the reaction materials are all in the slurry tank 13, so that the reaction materials in the slurry tank 13The density reaches 1.05-1.1g/cm 3 The circulation pump is then turned off, the circulation flow is stopped, and then the first transfer pump is turned on to transfer the reaction material in the slurry tank 13 to the flocculation basin 2.
In the system of the invention, a liquid level monitor is arranged at the position of the side wall of the flocculation and precipitation tank 2, which is close to the top, and when the reactant in the slurry tank 13 is conveyed into the flocculation and precipitation tank 2 through a pipeline under the action of a first conveying pump, the first conveying pump between the slurry tank 13 and the flocculation and precipitation tank 2 is forcibly closed when the reactant in the flocculation and precipitation tank 2 reaches the upper limit of the liquid level, and then flocculating agent is added into the flocculation and precipitation tank 2 to precipitate the reactant, thereby obtaining flocculated sediment.
In the system of the invention, the weight ratio of the reaction material to the amount of the flocculant is 1: (0.001-0.002). Specifically, the weight ratio of the reaction materials to the amount of the flocculant is 1:0.001, 1:0.0015 or 1:0.002.
in the system of the invention, the flocculant is one or more selected from anionic PAM (polyacrylamide), sodium dodecyl sulfate and anionic lignin. Preferably, the flocculant is anionic PAM.
In a specific embodiment of the present invention, in order to promote flocculation efficiency of the flocculant, a heater is provided inside the flocculation basin 2, and the heating temperature of the heater is 35-60 ℃, specifically, the heating temperature of the heater may be 35 ℃, 40 ℃, 45 ℃, 50 ℃, 55 ℃, or 60 ℃.
In a specific embodiment of the invention, the bottom of the flocculation basin 2 is arranged inclined with respect to the horizontal plane in order to facilitate the collection of flocculated sediment. In a preferred aspect of the invention, the angle θ between the bottom of the flocculation basin 2 and the horizontal is 5 ° -10 °. Specifically, the included angle θ between the bottom of the flocculation basin 2 and the horizontal plane may be 5 °, 8 °, or 10 °.
In a further preferred embodiment of the invention, in order to ensure that the flocculant and the reaction mass are sufficiently contacted for sedimentation, the flocculation basin 2 is internally provided with a low-speed stirrer, the stirring speed of which is 20-35rpm. Specifically, the stirring speed of the low-speed stirrer may be 20rpm, 25rpm, 30rpm or 35rpm.
In the system according to the invention, the sedimentation time is 0.5-1.5h, in particular the sedimentation time may be 0.5h, 1h or 1.5h.
In the system of the invention, a second conveying pump is connected between the flocculation sedimentation tank 2 and the cyclone separator 3, flocculated sediment obtained in the flocculation sedimentation tank 2 is conveyed into the cyclone separator 3 by the second conveying pump, the cyclone separator 3 is used for separating light phase components and heavy phase components contained in the flocculated sediment, the light phase components contain solution and a small amount of CaCO with small nucleation particle size 3 And CaSO 4 The heavy phase component contains CaCO with larger nucleation grain diameter 3 And CaSO 4 。
In the system according to the invention, the cyclone 3 comprises a first cyclone 31, a second cyclone 32 and a third cyclone 33; the bottom discharge port of the first cyclone separator 31 is connected with the feed port of the second cyclone separator 32, and the bottom discharge port of the second cyclone separator 32 is connected with the feed port of the third cyclone separator 33; the top discharge port of the first cyclone separator 31, the top discharge port of the second cyclone separator 32 and the top discharge port of the third cyclone separator 33 are respectively connected with the shower pipe 11. A third delivery pump is connected between the top discharge port of the first cyclone separator 31 and the spray pipe 11, a fourth delivery pump is connected between the top discharge port of the second cyclone separator 32 and the spray pipe 11, and a fifth delivery pump is connected between the top discharge port of the third cyclone separator 33 and the spray pipe 11.
In the system of the invention, flocculated sediment in the flocculation basin 2 is conveyed into the first cyclone separator 31 from a feed inlet of the first cyclone separator 31 by a second conveying pump, the flocculated sediment from the flocculation basin 2 is separated in the first cyclone separator 31, light phase components contained in the flocculated sediment are returned into the spray pipe 11 from a top discharge outlet of the first cyclone separator 31 by a third conveying pump for recycling, and heavy phase components in the flocculated sediment are conveyed into the second cyclone separator 32 from a feed inlet of the second cyclone separator 32 through a bottom discharge outlet of the first cyclone separator 31 under the action of gravity.
In the system of the present invention, since the heavy phase component from the first cyclone separator 31 also carries part of the light phase component, part of the light phase component in the second cyclone separator 32 flows back to the spray pipe 11 from the top discharge port of the second cyclone separator 32 through the fourth transfer pump for recycling, and the heavy phase component is transferred from the feed port of the third cyclone separator 33 to the third cyclone separator 33 through the bottom discharge port of the second cyclone separator 32 under the action of gravity.
In the system of the present invention, since the heavy phase component from the second cyclone 32 also carries a small amount of light phase component, the small amount of light phase component in the second cyclone 32 flows back to the spray pipe 11 from the top outlet of the third cyclone 33 through the fifth transfer pump for recycling, and the heavy phase component is transferred to the regeneration tank 4 from the bottom outlet of the third cyclone 33 under the action of gravity.
In the system of the invention, the flocculated sediment from the flocculation basin 2 can obtain better separation effect after three cyclone separation.
In the system according to the invention, the volume of the regeneration tank 4 is 25-30L. Specifically, the volume of the regeneration tank 4 may be 25L, 28L or 30L.
In the system according to the invention, the regeneration tank 4 contains a sulfuric acid solution, and the heavy phase component from the third cyclone 33 reacts with the sulfuric acid solution in the regeneration tank 4 to obtain CO 2 And gypsum suspension (containing CaSO) 4 Solid).
In the system according to the invention, the system further comprises a compressor 5, said compressor 5 being connected to the top of said regeneration tank 4, said compressor 5 being adapted to control the CO from said regeneration tank 4 2 Compression is performed.
In the system of the present invention, a pressure detection valve is provided on a pipe line connecting the regeneration tank 4 and the compressor 5. As the reaction in the regeneration tank 4 proceeds gradually, CO generated in the regeneration tank 4 2 Gradually increasing to cause the pressure in the regeneration tank 4 to gradually increase, and automatically opening the pressure detection valve when the pressure in the regeneration tank 4 reaches the predetermined pressure of the pressure detection valve, wherein CO generated in the regeneration tank 4 2 Is conveyed to the downstream compressor 5 through a pipeline for compression.
In the system according to the invention, the predetermined pressure of the pressure sensing valve is in the range of 0.11-0.12MPa. Specifically, the predetermined pressure range of the pressure detection valve may be 0.11MPa, 0.115MPa, or 0.12MPa.
In a specific embodiment of the present invention, the CO generated in the regeneration tank 4 is generated by 2 Usually with a small amount of moisture, whereas the CO 2 After treatment by the compressor 5, the CO 2 The water is still present and therefore the CO is required 2 Drying to obtain high-purity CO 2 The high purity CO 2 And then the product is conveyed to a product utilization end through a pipeline.
In a specific embodiment of the present invention, a liquid level control valve is disposed at the bottom of the regeneration tank 4. As the reaction in the regeneration tank 4 proceeds gradually, the gypsum suspension in the regeneration tank 4 increases gradually, the liquid level control valve is used for controlling the liquid level in the regeneration tank 4, and when the liquid level in the regeneration tank 4 exceeds 1/2 of the internal height of the regeneration tank 4, the liquid level control valve is opened to discharge the gypsum suspension in the regeneration tank 4.
In the system of the invention, the system also comprises a spray header 6 and a negative pressure transfer belt, the gypsum suspension in the regeneration tank 4 is conveyed to the spray header 6 through a pipeline, and the spray header 6 sprays the gypsum suspension onto the negative pressure transfer belt.
In a preferred embodiment of the invention, the bottom of the negative pressure transfer belt is provided with a suction filtration device, and gypsum is suspended The floating liquid is filtered to obtain high-quality gypsum material (CaSO) 4 Solids) and the filtrate.
In a further preferred embodiment of the invention, a sixth transfer pump is arranged between the suction filtration device and the flocculation basin 2, and the filtrate obtained after the gypsum suspension is subjected to suction filtration is transferred to the flocculation basin 2 by the sixth transfer pump for sedimentation again.
The second aspect of the present invention provides a flue gas co-processing method, which is implemented in the flue gas co-processing system, and comprises the following steps:
(1) Injecting slurry into the slurry tank 13 from the slurry inlet 16, and circularly conveying the slurry in the slurry tank 13 to the spray pipe 11 through a circulating pump for circular spraying;
(2) Introducing flue gas into the capturing tower 1 from the flue gas inlet 14, introducing ozone into the capturing tower 1 from the aeration port 12, and reacting the ozone, the flue gas and the slurry in the capturing tower 1 to obtain a reaction material; a heater is arranged in the capturing tower 1, and the flue gas contains NO x 、SO 2 And CO 2 ；
(3) The reaction materials are conveyed into a flocculation dropping tank 2 for sedimentation, then conveyed into a cyclone separator 3 for cyclone separation, and then conveyed into a regeneration tank 4 for reaction to obtain CO 2 And gypsum suspension; the regeneration tank 4 is filled with a sulfuric acid solution.
In the method of the invention, the flue gas contains NO x 、SO 2 And CO 2 The NO x Is NO and/or NO 2 NO in the flue gas x 、SO 2 And CO 2 The molar ratio of (2) is 1: (5-7): (270-350). In particular, NO in the flue gas x 、SO 2 And CO 2 The molar ratio of (2) may be 1:5: 270. 1:6:300 or 1:7:350.
in the method of the invention, the slurry is Ca (OH) 2 Suspension, ca (OH) 2 The suspension had a concentration of 6-8wt.%. Specifically, the Ca (OH) 2 The concentration of the suspension may be 6wt.%, 7wt.%, 8wt.%.
In the method of the present invention, the Ca (OH) 2 The volume ratio of the suspension to the flue gas to the ozone is 1: (23.33-23.34): (0.51-0.52). Specifically, the Ca (OH) 2 The volume ratio of suspension, flue gas and ozone may be 1:23.33:0.51 or 1:23.34:0.52.
in the process according to the invention, in step (2), the temperature of the reaction is 40-70 ℃, in particular, the temperature of the reaction may be 40 ℃, 50 ℃, 60 ℃ or 70 ℃.
In the method of the present invention, the reaction occurring in step (2) comprises:
SO 2 +2OH - ——SO 3 2- +H 2 O；
SO 3 2- +O 3 ——SO 4 2- +O 2 ；
SO 3 2- +O 2 ——SO 4 2- ；
NO+O 3 ——NO 2 +O 2 ；
NO+O 2 ——NO 2 ；
4NO 2 +2H 2 O+O 2 ——4HNO 3 ；
CO 2 +2OH - ——CO 3 2- +H 2 O；
Ca 2+ +SO 4 2- ——CaSO 4 ；
Ca 2+ +CO 3 2- ——CaCO 3 。
in the method of the present invention, NO contained in the flue gas after the reaction in step (2) is completed x Conversion to HNO 3 SO contained in the flue gas 2 Conversion to CaSO 4 CO contained in the flue gas 2 Conversion to CaCO 3 。
In the process according to the invention, in step (2), the reaction mass contains CaSO 4 And CaCO (CaCO) 3 。
In the method according to the invention, in step (3), the regeneration tank 4 contains a sulfuric acid solution, the concentration of which is 20-40wt.%. In particular, the concentration of the sulfuric acid solution may be 20wt.%, 30wt.%, or 40wt.%.
In the preferred case of the invention, the sulfuric acid solution contained in the regeneration tank 4 ensures complete reaction with the heavy phase components from the cyclone 3.
In the method of the invention, the volume of the sulfuric acid solution contained in the regeneration tank 4 is 5-8L. Specifically, the volume of the sulfuric acid solution contained in the regeneration tank 4 may be 5L, 6L, 7L or 8L.
In the method of the present invention, in step (3), the reaction conditions include: the temperature is 30-40deg.C, and the time is 15-30min.
In the method of the present invention, the reaction occurring in step (3) comprises: caCO (CaCO) 3 +2H + +SO 4 2- ——CaSO 4 +CO 2 +H 2 O。
In the specific embodiment of the present invention, in the step (3), the regeneration tank 4 contains H 2 SO 4 And CaCO contained in the heavy phase component from the cyclone 3 3 Carrying out reaction to obtain CO 2 And gypsum suspension, said CO 2 Delivering to the compressor 5 for compression and then drying to obtain high-purity CO 2 The gypsum suspension is suction filtered to obtain a gypsum material (CaSO 4 Solids) and filtrate.
In particular embodiments of the present invention, there are no particular requirements on the drying apparatus, which may be conventional in the art, for example, a filtration vessel containing a desiccant filler (e.g., silica gel, molecular sieve, etc.).
In a specific embodiment of the invention, the filtrate also contains SO 4 2- For efficient recovery of gypsum material, the filtrate is returned to the flocculation basin 2 for continued sedimentation.
In a specific embodiment of the present invention, the method comprises the following steps ofThe slurry inlet 16 injects Ca (OH) into the slurry tank 13 2 Suspension, start the stirrer in the slurry tank 13; then starting a circulating pump, wherein the slurry in the slurry tank 13 is conveyed to the spraying pipe 11 through a pipeline under the action of the circulating pump, the spraying pipe 11 sprays the slurry downwards, and the slurry circularly flows between the slurry tank 13 and the spraying pipe 11; turning on a heater inside the capturing tower 1 (the pressure inside the capturing tower 1 is normal pressure), and when the temperature inside the capturing tower 1 is stable, introducing flue gas (containing NO) into the capturing tower 1 from the flue gas inlet 14 x 、SO 2 CO 2 ) Ozone is introduced into the capturing tower 1 from the aeration port 12; ca (OH) 2 The suspension reacts with the flue gas and ozone to obtain a reaction material (all the reaction material is gathered in the slurry tank 13), and the reaction material contains CaSO 4 And CaCO (CaCO) 3 The method comprises the steps of carrying out a first treatment on the surface of the When the density of the liquid slurry in the slurry tank 13 reaches 1.05-1.1g/cm 3 Then, the circulating pump is closed, the circulating flow is stopped, then the first conveying pump is started, the reactant in the slurry tank 13 is conveyed into the flocculation tank 2 through a pipeline, and a small amount of NO which does not participate in the reaction in the capturing tower 1 is captured x 、SO 2 、CO 2 And other components contained in the flue gas are discharged from the exhaust port 15; when the reaction material in the flocculation drop tank 2 reaches the upper limit of the liquid level, a first conveying pump between the pulp tank 13 and the flocculation drop tank 2 is closed, a heater in the flocculation drop tank 2 is started at the moment, when the temperature in the flocculation drop tank 2 is stable, a flocculating agent (anionic PAM) is added into the flocculation drop tank 2 for sedimentation, and flocculated sediment (the flocculated sediment contains a light phase component and a heavy phase component, the light phase component contains a solution and a small amount of CaCO with smaller nucleation particle size) is obtained at the bottom of the flocculation drop tank 2 3 And CaSO 4 The heavy phase component contains CaCO with larger nucleation grain diameter 3 And CaSO 4 ) The method comprises the steps of carrying out a first treatment on the surface of the The flocculated sediment at the bottom of the flocculation basin 2 is conveyed into the first cyclone separator 31 from the feed inlet of the first cyclone separator 31 by a second conveying pump, the flocculated sediment from the flocculation basin 2 is separated in the first cyclone separator 31, and the light phase component contained in the flocculated sediment is conveyed from the first cyclone separator 31 by a third conveying pumpThe top discharge port of the first cyclone separator 31 flows back to the spray pipe 11 for recycling, and heavy phase components in flocculated sediment are conveyed into the second cyclone separator 32 from the feed port of the second cyclone separator 32 through the bottom discharge port of the first cyclone separator 31 under the action of gravity; since the heavy phase component from the first cyclone separator 31 also carries part of the light phase component, part of the light phase component in the second cyclone separator 32 flows back to the spray pipe 11 from the top discharge port of the second cyclone separator 32 through the fourth conveying pump for recycling, and the heavy phase component is conveyed from the feed port of the third cyclone separator 33 to the third cyclone separator 33 through the bottom discharge port of the second cyclone separator 32 under the action of gravity; since the heavy phase component from the second cyclone separator 32 also carries a small amount of light phase component, the small amount of light phase component in the second cyclone separator 32 flows back to the spray pipe 11 from the top discharge port of the third cyclone separator 33 through the fifth delivery pump for recycling, and the heavy phase component is delivered to the regeneration tank 4 from the bottom discharge port of the third cyclone separator 33 under the action of gravity; adding H to the regeneration tank 4 2 SO 4 Solution H 2 SO 4 With CaCO contained in the heavy phase component 3 Reacting to obtain CO 2 Gas and gypsum suspension (containing CaSO) 4 Solids) as the reaction in the regeneration tank 4 proceeds, the CO generated in the regeneration tank 4 2 Gradually increasing to cause the pressure in the regeneration tank 4 to gradually increase, and automatically opening a pressure detection valve after the pressure in the regeneration tank 4 reaches 0.11-0.12MPa, wherein CO is generated in the regeneration tank 4 2 Is conveyed to a downstream compressor 5 for compression through a pipeline, and CO after compression 2 Usually with a small amount of moisture, said CO containing a small amount of moisture 2 Drying to obtain high-purity CO 2 The high purity CO 2 Conveying the product to a product utilization end through a pipeline; as the reaction in the regeneration tank 4 proceeds gradually, the gypsum suspension in the regeneration tank 4 increases gradually, and when the liquid level in the regeneration tank 4 exceeds 1/2 of the internal height of the regeneration tank 4, the liquid is openedThe position control valve is used for conveying the gypsum suspension in the regeneration tank 4 to the spray header 6 through a pipeline, the spray header 6 sprays the gypsum suspension onto the negative pressure transfer belt, and the gypsum suspension is processed by the suction filtration device at the bottom of the negative pressure transfer belt to obtain a high-quality gypsum material (CaSO) 4 Solids) and filtrate; and the filtrate is conveyed into the flocculation basin 2 through a sixth conveying pump for sedimentation again.
The present invention will be described in detail by examples. The flue gas co-treatment method of the following embodiment is performed in a flue gas co-treatment system shown in fig. 1, wherein the flue gas co-treatment system comprises a capturing tower 1, a flocculation basin 2, a cyclone separator 3 and a regeneration tank 4 which are sequentially communicated along the material trend; the capturing tower 1 is provided with a flue gas inlet 14, an exhaust port 15 and a slurry inlet 16, a spray pipe 11 is arranged above the inside of the capturing tower 1, and a slurry tank 13 is arranged below the inside of the capturing tower 1; a stirrer is arranged in the slurry tank 13; a density monitor is arranged at the outlet of the slurry tank 13; the capturing tower 1 is also provided with a circulating pump; the bottom of the capturing tower 1 is provided with a plurality of aeration openings 12; the number of the aeration openings 12 is 6; 6 aeration openings 12 are arranged at the bottom of the capturing tower 1 in concentric circles; the bottom of the flocculation dropping pond 2 is obliquely arranged relative to the horizontal plane; the included angle theta between the bottom of the flocculation dropping pool 2 and the horizontal plane is 8 degrees; a liquid level monitor is arranged at the position of the flocculation dropping pool 2 close to the top; the cyclone 3 comprises a first cyclone 31, a second cyclone 32 and a third cyclone 33; the bottom discharge port of the first cyclone separator 31 is connected with the feed port of the second cyclone separator 32, and the bottom discharge port of the second cyclone separator 32 is connected with the feed port of the third cyclone separator 33; the top discharge port of the first cyclone separator 31, the top discharge port of the second cyclone separator 32 and the top discharge port of the third cyclone separator 33 are respectively connected with the spray pipe 11; the bottom of the regeneration tank 4 is provided with a liquid level control valve; the system also comprises a compressor 5, a spray header 6 and a negative pressure transfer belt, wherein a pressure detection valve is arranged on a pipeline connected with the regeneration tank 4 and the compressor 5, and a heater is arranged in the capture tower 1; a heater is arranged in the flocculation dropping pond 2; a low-speed stirrer is arranged in the flocculation dropping pond 2; the outlet of the pulp tank 13 is connected with the flocculation dropping tank 2 through a pipeline, and a first conveying pump is arranged on the pipeline; a second delivery pump is connected between the flocculation dropping tank 2 and the cyclone separator 3; a third conveying pump is connected between the top discharge port of the first cyclone separator 31 and the spray pipe 11, a fourth conveying pump is connected between the top discharge port of the second cyclone separator 32 and the spray pipe 11, and a fifth conveying pump is connected between the top discharge port of the third cyclone separator 33 and the spray pipe 11; a sixth conveying pump is arranged between the suction filtration device and the flocculation dropping pond 2.
The normal pressure in the following examples is referred to as 100kpa and the test results are shown in table 1.
Example 1
(1) 10L of Ca (OH) was injected into the slurry tank 13 from the slurry inlet 16 2 Suspension (Ca (OH) 2 The concentration of the suspension was 7 wt.%), the stirrer in the slurry tank 13 was started, and the stirring speed was 50rpm; then starting a circulating pump, wherein the slurry in the slurry tank 13 is conveyed to the spraying pipe 11 through a pipeline under the action of the circulating pump, the spraying pipe 11 sprays the slurry downwards, and the slurry circularly flows between the slurry tank 13 and the spraying pipe 11;
(2) Turning on a heater inside the capturing tower 1 (the pressure inside the capturing tower 1 is normal pressure), setting the heating temperature to be 50 ℃, and introducing 233.3L of flue gas (containing NO) into the capturing tower 1 from the flue gas inlet 14 when the temperature inside the capturing tower 1 is stabilized at 50 DEG C x 、SO 2 CO 2 NO in the flue gas x 、SO 2 And CO 2 The molar ratio of (2) is 1:6:300 5.1L of ozone is introduced into the capturing tower 1 from the aeration port 12; ca (OH) 2 The suspension reacts with the flue gas and ozone to obtain a reaction material (all the reaction material is gathered in the slurry tank 13), and the reaction material contains CaSO 4 And CaCO (CaCO) 3 The method comprises the steps of carrying out a first treatment on the surface of the When the slurry density in the slurry tank 13 reached 1.1g/cm 3 After that, the circulation pump is turned off, the circulation flow is stopped, and then the first delivery pump is turned on, saidThe reaction material in the slurry tank 13 is conveyed into the flocculation dropping tank 2 through a pipeline, and a small amount of NO which does not participate in the reaction in the tower 1 is captured x 、SO 2 、CO 2 And other components contained in the flue gas are discharged from the exhaust port 15;
(3) When the reaction material in the flocculation drop tank 2 reaches the upper limit of the liquid level, a first conveying pump between the pulp tank 13 and the flocculation drop tank 2 is closed, a heater in the flocculation drop tank 2 is started, the heating temperature is set to 35 ℃, when the temperature in the flocculation drop tank 2 is stabilized at 35 ℃, a flocculating agent (anionic PAM) is added into the flocculation drop tank 2 for sedimentation (the weight ratio of the reaction material to the dosage of the flocculating agent is 1:0.015), the sedimentation time is 60min, and flocculation sediment (the flocculation sediment contains a light phase component and a heavy phase component and contains a solution and a small amount of CaCO with smaller nucleation particle size) is obtained at the bottom of the flocculation drop tank 2 3 And CaSO 4 The heavy phase component contains CaCO with larger nucleation grain diameter 3 And CaSO 4 ）；
(4) The flocculated sediment at the bottom of the flocculation basin 2 is conveyed into the first cyclone separator 31 from the feed inlet of the first cyclone separator 31 by a second conveying pump, the flocculated sediment from the flocculation basin 2 is separated in the first cyclone separator 31, the light phase component contained in the flocculated sediment is returned into the spray pipe 11 from the top discharge outlet of the first cyclone separator 31 by a third conveying pump for recycling, and the heavy phase component in the flocculated sediment is conveyed into the second cyclone separator 32 from the feed inlet of the second cyclone separator 32 through the bottom discharge outlet of the first cyclone separator 31 under the action of gravity; since the heavy phase component from the first cyclone separator 31 also carries part of the light phase component, part of the light phase component in the second cyclone separator 32 flows back to the spray pipe 11 from the top discharge port of the second cyclone separator 32 through the fourth conveying pump for recycling, and the heavy phase component is conveyed from the feed port of the third cyclone separator 33 to the third cyclone separator 33 through the bottom discharge port of the second cyclone separator 32 under the action of gravity; since the heavy phase component from the second cyclone separator 32 also carries a small amount of light phase component, the small amount of light phase component in the second cyclone separator 32 flows back to the spray pipe 11 from the top discharge port of the third cyclone separator 33 through the fifth transfer pump for recycling, and the heavy phase component is transferred to the regeneration tank 4 from the bottom discharge port of the third cyclone separator 33 under the action of gravity.
(5) Adding 6L H to the regeneration tank 4 2 SO 4 Solution (H) 2 SO 4 Concentration of solution was 30 wt.%), H 2 SO 4 With CaCO contained in the heavy phase component 3 Reacting to obtain CO 2 Gas and gypsum suspension (containing CaSO) 4 Solids) as the reaction in the regeneration tank 4 proceeds, the CO generated in the regeneration tank 4 2 Gradually increasing to cause the pressure in the regeneration tank 4 to gradually increase, and automatically opening a pressure detection valve when the pressure in the regeneration tank 4 reaches 0.115MPa, wherein CO is generated in the regeneration tank 4 2 Is conveyed to a downstream compressor 5 for compression through a pipeline, and CO after compression 2 Usually with a small amount of moisture, said CO containing a small amount of moisture 2 Drying to obtain high-purity CO 2 The high purity CO 2 Conveying the product to a product utilization end through a pipeline; as the reaction in the regeneration tank 4 proceeds, the gypsum suspension in the regeneration tank 4 increases gradually, when the liquid level in the regeneration tank 4 exceeds 1/2 of the internal height of the regeneration tank 4, a liquid level control valve is opened to convey the gypsum suspension in the regeneration tank 4 to a spray head 6 through a pipeline, the spray head 6 sprays the gypsum suspension onto a negative pressure transfer belt, and after the gypsum suspension is processed by a suction filtration device at the bottom of the negative pressure transfer belt, a high quality gypsum material (CaSO 4 Solids) and filtrate; and the filtrate is conveyed into the flocculation basin 2 through a sixth conveying pump for sedimentation again.
Example 2
The procedure of example 1 was followed, except that the volume of ozone introduced into the capturing column 1 in example 2 was 4.7L.
Example 3
The procedure of example 1 was followed, except that in example 3, the volume of ozone introduced into the capturing column 1 was 5.4L.
Comparative example 1
The procedure of example 1 was followed, except that comparative example 1 was not provided with aeration port 12, and ozone was not introduced into capturing column 1.
Comparative example 2
The procedure of example 1 was followed except that comparative example 2 did not use a heater in the capturing column 1.
Comparative example 3
According to the method of example 1, except that comparative example 3 was added to the regeneration tank 4 with H 2 SO 4 HCl solutions with equal volumes and concentrations.
Comparative example 4
The procedure of example 1 is followed, except that the flue gas contains SO 2 And NO x Does not contain CO 2 。
Comparative example 5
The procedure of example 1 is followed, except that the flue gas contains SO 2 And CO 2 NO-containing x 。
Test example 1
The split flow and concentration of the inlet and outlet gas groups of the capturing tower are measured by a flue gas analyzer, and the flow is Q respectively in And Q out The concentration is C respectively in And C out The removal efficiency is eta, and eta= (Q) in -Q out ）/Q in The flue gas removal efficiency can be calculated.
Test example 2
Measuring regeneration tank outlet exhaust CO using mass flow meter 2 Flow rate available CO 2 A volume value; the gypsum mass can weigh the gypsum product deposited downstream of the negative pressure transfer belt.
TABLE 1
Comparative example 1, example 2, example 3, example 2 was purged with ozone containingThe amount of CO was small compared with example 1 2 Volume, caSO 4 The quality and flue gas removal efficiency are both reduced, the ozone content is too much in example 3, compared with example 1, the CO 2 Volume, caSO 4 The quality and the flue gas removal efficiency are almost unchanged, so that the ozone content introduced into the system is proper.
Comparative example 1 and comparative example 1, if ozone is not introduced into the capturing column, no ozone participates in the reaction in the system, resulting in CO 2 Volume reduction, caSO 4 The quality is reduced, and the flue gas removal efficiency is reduced; comparative example 1 and comparative example 2, the heater, ca (OH), was not used in the capturing column 1 2 Solubility decreases, system internal reference reacts with Ca (OH) 2 Reduction of CO 2 Reduced volume, caSO 4 The quality is reduced, and the flue gas removal efficiency is reduced; comparative examples 1 and 3, added to the regeneration tank 4 is a solution of HCl, HCl and CaSO 4 Reaction to cause CaSO 4 The quality is rapidly reduced; comparative examples 1 and 4, 5, the absence of a contaminant of a certain type in comparative examples 4, 5 has a certain influence on the excitation of the reaction process, thus the removal efficiency is reduced, CO 2 Or CaSO 4 The gypsum yield decreases.
As can be seen from the results in Table 1, the flue gas collaborative treatment system of the invention is used for carrying out flue gas collaborative treatment, and the SO in the tower is captured 2 、NO x 、CO 2 The removal efficiency can reach 96 percent, and the synergistic removal effect is good; the collaborative removal system saves equipment occupation and investment and has obvious technical advantages.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.

Claims (10)

1. The flue gas cooperative treatment system is characterized by comprising a capturing tower (1), a flocculation dropping pond (2), a cyclone separator (3) and a regeneration tank (4) which are sequentially communicated along the material trend;
The capturing tower (1) is provided with a flue gas inlet (14), an exhaust port (15) and a slurry inlet (16), a spray pipe (11) is arranged above the inside of the capturing tower (1), a slurry tank (13) is arranged below the inside of the capturing tower (1), and the slurry inlet (16) is used for injecting slurry into the slurry tank (13); the capturing tower (1) is also provided with a circulating pump, and the circulating pump is used for circularly conveying the slurry in the slurry tank (13) into the spray pipe (11) for circulating spraying;
a heater is arranged in the capturing tower (1), a plurality of aeration openings (12) are formed in the bottom of the capturing tower (1), the aeration openings (12) are used for introducing ozone into the capturing tower (1), and the ozone and the flue gas react with the slurry in the capturing tower (1); the flue gas contains NO x 、SO 2 And CO 2 。
2. The system according to claim 1, characterized in that the number of aeration openings (12) is 3-6;
preferably, a plurality of the aeration openings (12) are arranged at the bottom of the capturing tower (1) in concentric circles.
3. System according to claim 1, characterized in that the bottom of the flocculation basin (2) is arranged inclined with respect to the horizontal plane;
Preferably, the included angle theta between the bottom of the flocculation dropping pond (2) and the horizontal plane is 5-10 degrees.
4. The system according to claim 1, characterized in that the cyclone separator (3) comprises a first cyclone separator (31), a second cyclone separator (32) and a third cyclone separator (33);
preferably, a bottom discharge port of the first cyclone separator (31) is connected with a feed port of the second cyclone separator (32), and a bottom discharge port of the second cyclone separator (32) is connected with a feed port of the third cyclone separator (33);
preferably, the top discharge port of the first cyclone separator (31), the top discharge port of the second cyclone separator (32) and the top discharge port of the third cyclone separator (33) are respectively connected with the spray pipe 11.
5. The system according to claim 1, further comprising a compressor (5), said compressor (5) being connected to the top of the regeneration tank (4), said compressor (5) being adapted to compress CO from the regeneration tank (4) 2 。
6. The system according to claim 1, further comprising a shower head (6) and a negative pressure transfer belt, the shower head (6) being adapted to shower gypsum suspension from the regeneration tank (4) onto the negative pressure transfer belt.
7. A flue gas co-processing method implemented in a flue gas co-processing system according to any one of claims 1 to 6, characterized in that the method comprises the steps of:
(1) Injecting slurry into the slurry tank (13) from the slurry inlet (16), and circularly conveying the slurry in the slurry tank (13) into the spray pipe (11) through a circulating pump for circular spraying;
(2) Introducing flue gas into the capturing tower (1) from the flue gas inlet (14), introducing ozone into the capturing tower (1) from the aeration port (12), and reacting the ozone and the flue gas with the slurry in the capturing tower (1) to obtain a reaction material; a heater is arranged in the capturing tower (1), and the flue gas contains NO x 、SO 2 And CO 2 ；
(3) The reaction materials are conveyed into a flocculation dropping tank (2)Settling, transferring to the cyclone separator (3) for cyclone separation, transferring to the regeneration tank (4) for reaction to obtain CO 2 And gypsum suspension; the regeneration tank (4) is filled with a sulfuric acid solution.
8. The process of claim 7, wherein in step (2), the reaction temperature is 40-70 ℃.
9. The method of claim 7, wherein in step (3), the concentration of the sulfuric acid solution is 20-40wt.%;
preferably, in step (3), the reaction conditions include: the temperature is 30-40deg.C, and the time is 15-30min.
10. The method of claims 7-9, wherein the slurry is Ca (OH) 2 A suspension;
preferably, the Ca (OH) 2 The suspension had a concentration of 6-8wt.%;
preferably, the Ca (OH) 2 The volume ratio of the suspension to the flue gas to the ozone is 1: (23.33-23.34): (0.51-0.52).
CN202311401637.7A 2023-10-26 2023-10-26 Flue gas cooperative treatment system and flue gas cooperative treatment method Pending CN117482739A (en)

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