CN114904369A - Combined packing absorption tower and flue gas purification process - Google Patents

Combined packing absorption tower and flue gas purification process Download PDF

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Publication number
CN114904369A
CN114904369A CN202210739769.XA CN202210739769A CN114904369A CN 114904369 A CN114904369 A CN 114904369A CN 202210739769 A CN202210739769 A CN 202210739769A CN 114904369 A CN114904369 A CN 114904369A
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Prior art keywords
packing
foam
absorption tower
area
liquid
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Chinese (zh)
Inventor
邱明英
张亚志
崔岩
朱繁
徐继法
李加旺
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MCC Capital Engineering and Research Incorporation Ltd
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MCC Capital Engineering and Research Incorporation Ltd
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Priority to CN202210739769.XA priority Critical patent/CN114904369A/en
Publication of CN114904369A publication Critical patent/CN114904369A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B01D53/185—Liquid distributors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/14—Packed scrubbers
    • 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
    • B01D53/1406—Multiple stage absorption
    • 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
    • B01D53/1412—Controlling the absorption process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/30—Loose or shaped packing elements, e.g. Raschig rings or Berl saddles, for pouring into the apparatus for mass or heat transfer
    • 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
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/302—Basic shape of the elements
    • B01J2219/30203—Saddle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/302—Basic shape of the elements
    • B01J2219/30215—Toroid or ring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30491—Foam like materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/31—Size details
    • B01J2219/315—Two or more types of packing elements or packing elements of different sizes present in the column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/332—Details relating to the flow of the phases
    • B01J2219/3325—Counter-current flow
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention provides a combined packing absorption tower and a flue gas purification process, wherein the absorption tower comprises a single tower structure or a double tower structure, and when the absorption tower is of the single tower structure, the absorption tower comprises a spraying reaction area, an air flow uniform distribution area and a foam reaction area, wherein the spraying reaction area is positioned at the bottom of the absorption tower, the air flow uniform distribution area and the foam reaction area are arranged at the upper part of the spraying reaction area side by side, and the bottom and the top of the air flow uniform distribution area are respectively communicated with the top of the spraying reaction area and the top of the foam reaction area; when the double-tower structure is adopted, the double-tower structure comprises a first absorption tower and a second absorption tower which are communicated through a pipeline; the spraying reaction area or the first absorption tower is internally provided with a liquid storage area, an air inlet pipe, a packing layer and a liquid distributor from bottom to top, the air flow uniform distribution area comprises a flue and a first fog drop generator arranged at the top of the flue, and the foam reaction area or the second absorption tower is internally provided with a second fog drop generator, a plurality of micropore filling sections, a liquid-foam mixed phase area, an air outlet pipe and a temporary liquid storage area from top to bottom.

Description

Combined packing absorption tower and flue gas purification process
Technical Field
The invention relates to a combined filler absorption tower and a purification process of flue gas, belonging to the technical field of chemical environment-friendly equipment.
Background
At present, the alcohol amine method is the most widely applied desulfurization and decarburization process, and the tower is an important mass transfer and heat transfer separation device. The packed tower has the advantages of easy manufacture and replacement, wide material range, strong adaptability, energy conservation and the like, and the separation performance is superior to that of a plate tower in most cases, so the packed tower is increasingly applied to the alcohol amine process. The packing is a core component of the packed tower, and the mass transfer efficiency of the packing is directly related to the operating performance of the packed tower. Fixed fillers have the following disadvantages: in the packed tower, the gas phase and the solid phase are in countercurrent contact, the contact time of the surfaces of the gas phase and the solid phase is too short, the specific surface area of the packing is fixed, the height of the packing can only be increased in order to increase the mass transfer area and the reaction time, and the investment cost is greatly increased at the moment; the limited liquid wettability is determined by the fixed and unchangeable material, geometric structure, parameters and the like of the filler, and the liquid film is turbulent and the mass transfer efficiency is limited. The design of the tower in the future requires that the tower equipment has excellent comprehensiveness such as high flux, high efficiency, low pressure drop and the like, and the important points are how to improve the mass transfer efficiency of the filler, how to increase the specific surface area of the filler, improve the surface utilization rate, improve the diffusion coefficient, reduce the thickness of a stagnant flow film layer and the like.
Prior art related to the present invention:
the technical scheme of the prior art I is as follows:
chinese patent CN102698550A discloses a foam and filler integrated furnace gas purification tower, which combines the traditional filler tower and foam tower into a whole, and solves the problems of large resistance, low dust removal efficiency and general purification effect in the industrial sulfuric acid production process.
The first prior art has the following defects:
(1) in the absorption unit, the gas-liquid directly contacts and reacts in the filler to cause phenomena of entrainment, bubbling, channeling, overflow and the like of the absorbent in the operation process;
(2) the gas phase and the solid phase are in countercurrent contact, so that the size of the trapping equipment is large and the investment cost is high in order to improve the absorption and mass transfer rate of the gas phase and the solid phase.
The second prior art related to the present invention:
the technical scheme of the prior art II is as follows:
chinese patent CN103370119A discloses a vertical and horizontal absorber which uses solvent foam to absorb carbon dioxide, forms foam through multiple screen arrays and breaks the foam repeatedly to form a rapidly changing absorption surface, improving the surface area of mass transfer and significantly increasing absorption efficiency.
The second prior art has the following defects:
(1) the absorption process is an exothermic reaction, and in the process of continuously breaking and regenerating a liquid film on the surface of foam, the temperature is increased, the breaking and regenerating frequency of the liquid film is gradually reduced, and the absorption and mass transfer effects are influenced;
(2) the foam directional ordered collision and rupture process can form a liquid film locally by only depending on the regular foam mass transfer technology, and the problems of large filling resistance and easy blockage exist.
Therefore, it has become an urgent technical problem in the art to provide a novel combined packed absorption tower and flue gas purification process.
Disclosure of Invention
In order to overcome the defects and shortcomings of the absorption tower in the prior art, such as large packing volume, high cost, large resistance of the regular foam mass transfer technology, easy blockage, no temperature control measure and the like, the invention aims to provide a combined packing absorption tower.
It is also an object of the present invention to provide a process for the purification of flue gases.
In order to achieve the above object, in one aspect, the present invention provides a combined packed absorption tower, wherein the combined packed absorption tower comprises a single tower structure or a double tower structure, and when the combined packed absorption tower is a single tower structure, the combined packed absorption tower comprises a spray reaction zone, an air flow uniform distribution zone and a foam reaction zone, the spray reaction zone is located at the bottom of an absorption tower, the air flow uniform distribution zone and the foam reaction zone are arranged side by side at the upper part of the spray reaction zone, and the bottom and the top of the air flow uniform distribution zone, i.e. the bottom and the top of a flue, are respectively communicated with the top of the spray reaction zone and the top of the foam reaction zone;
the spraying reaction area is provided with a liquid storage area, an air inlet pipe, a packing layer and a liquid distributor from bottom to top, wherein one side of the liquid storage area is provided with a liquid outlet, one side of the air inlet pipe is provided with an air inlet, the air flow uniform distribution area comprises a flue and a first fog drop generator arranged at the top of the flue, and the foam reaction area is provided with a second fog drop generator, a plurality of micropore filling sections, a liquid-foam mixed phase area, an air outlet pipe and a temporary liquid storage area from top to bottom;
when the combined type filler absorption tower is of a double-tower structure, the combined type filler absorption tower comprises a first absorption tower and a second absorption tower, the first absorption tower and the second absorption tower are communicated through a pipeline, a liquid storage area, an air inlet pipe, a packing layer and a liquid distributor are arranged in the first absorption tower from bottom to top, and a second fog drop generator, a plurality of micropore packing sections, a liquid-foam mixed phase area, an air outlet pipe and a temporary liquid storage area are arranged in the second absorption tower from top to bottom.
In the invention, the filler layer used in the spraying reaction zone is a filler layer formed by conventional fillers, and can be reasonably selected according to the actual operation needs on site as long as the aim of the invention can be realized.
In an embodiment of the above combined packed absorption tower of the present invention, the number of the first droplet generators may be one or more.
In an embodiment of the above combined packed absorption column of the present invention, the liquid outlet of the temporary liquid storage region is communicated with the liquid distributor via a circulation pump via a return pipe.
As a specific embodiment of the above combined packed absorption tower of the present invention, the flue inlet at the junction of the bottom of the flue and the spray reaction zone is a right-angled triangle structure, and the oblique side of the right-angled triangle structure is connected to the tower wall on the opposite side of the flue. The invention adopts the flue inlet with the right-angled triangle structure, so that the resistance in the gas transmission process can be reduced.
As a specific embodiment of the above combined packing absorption tower of the present invention, a flue inlet at a junction between the top of the flue and the foam reaction zone is further provided with a flow guide plate and a flow rectification grid respectively for guiding the gas in the flue to the foam reaction zone.
As a specific embodiment of the above combined packed absorption tower of the present invention, the top elbow of the flue is provided with a flow guide plate, the flue inlet at the top of the foam reaction zone/the flue outlet at the top of the airflow uniform distribution zone is of a delta wing structure, a layer of rectification grids is arranged at the intersection of the delta wing structure and the tower wall, and a second mist generator is further arranged below the rectification grids.
As a specific embodiment of the above-mentioned combined packing absorption tower of the present invention, the plurality of microporous packing sections include an upper layer of packing, a lower layer of packing, and a foam generation region formed between the upper layer of packing and the lower layer of packing, wherein the upper layer of packing is ordered and regular microporous mesh plate structured packing, the lower layer of packing is disordered porous silicon carbide packing, and the pore diameters of the upper layer of packing and the lower layer of packing are different.
As a specific embodiment of the above combined packing absorption tower, the upper layer of packing is U-shaped micropore net plate structured packing, the wave crests, the wave troughs and the side wall plates are uniformly distributed with meshes with the diameter of less than 0.05mm, and the lower layer of packing is nonmetal porous foam silicon carbide packing with the diameter of 1-2 mm.
As a specific embodiment of the above combined packing absorption tower of the present invention, the upper packing and the lower packing respectively comprise a grid support structure formed by support rods, each grid is internally provided with a circular packing ring, the packing is filled in the circular packing ring, and a gap between the grid and the circular packing ring is filled with a water-resistant material;
the number of the second fog drop generators is the same as that of the circular packing rings, and the centers of the nozzles of the second fog drop generators are opposite to the centers of the circular packing rings.
In a specific embodiment of the above combined packed absorption tower of the present invention, the number of the circular packing rings in the upper packing and the lower packing is the same.
As a specific embodiment of the combined packing absorption tower, the number of the circular packing rings is more than or equal to 4.
As a specific embodiment of the above-mentioned combined packed absorption tower of the present invention, a water-blocking weir is disposed at the outer side of the microporous packing section, i.e. at the edge of the microporous packing section near the tower wall side, the water-blocking weir is connected to the upper layer of packing and the lower layer of packing respectively towards the side/vertical surface of the microporous packing section, the upper end of the water-blocking weir is slightly higher than the upper layer of packing, the side/vertical surface of the water-blocking weir facing away from the microporous packing section is connected to the inner side wall of the foam reaction zone through a horizontal connection section, and an overflow section is formed between the side of the water-blocking weir facing away from the microporous packing section and the inner side wall of the foam reaction zone.
In an embodiment of the above combined packed absorption tower of the present invention, the horizontal connection section is made of a microporous packing material, and the material of the horizontal connection section is the same as that of the upper layer of packing material, that is, in some embodiments of the present invention, the material of the horizontal connection section may be a U-shaped microporous mesh plate structured packing material.
As a specific embodiment of the above-mentioned combined packing absorption tower of the present invention, the side/vertical surface of the water-blocking weir facing away from the microporous packing section is connected to the inner sidewall of the foam reaction zone through two horizontal connecting sections which are parallel to each other and located at the same height as the upper-layer packing and the lower-layer packing.
In a specific embodiment of the present invention, the packed absorption tower is a packed absorption tower, wherein the foam generating zone has a venturi structure.
In a specific embodiment of the above combined packed absorption tower of the present invention, the venturi tube structure is externally wound with multiple turns of venturi cooling coils from top to bottom.
In some embodiments of the invention, the cooling medium that may be used in the venturi cooling coil may be water, air, or other common coolants.
As a specific embodiment of the above combined packing absorption tower of the present invention, wherein the number of the microporous packing sections is n +1, wherein n is an integer no less than 1;
and a foam free mixing area is formed between the adjacent microporous filler sections.
As a specific embodiment of the above combined packing absorption tower of the present invention, a plurality of retractable nozzles are disposed below the lower packing, and can be retracted to the edge of the tower wall.
In some embodiments of the present invention, the medium used/sprayed by the retractable spray head is compressed air or superheated steam.
In the invention, after the combined packing absorption tower runs for a period of time, packing in a foam reaction zone can be blocked, so that the pressure drop in the tower is overlarge. The telescopic shower nozzle that the filler below of lower floor was equipped with can start this moment, packs to the upper strata and packs to carry out simply, sweep fast with lower floor, under compressed air or superheated steam's effect, packs the hole and blocks up and to obtain the mediation.
In a specific embodiment of the above combined packed absorption tower of the present invention, the air inlet end of the air outlet pipe faces downward and is provided with a wire mesh demister.
In a specific embodiment of the above combined packed absorption tower of the present invention, the orifice diameter of the wire mesh demister is 3 mm.
In the invention, the air inlet end of the air outlet pipe faces downwards and is provided with the silk screen demister, so that the purified gas of the foam layer can be effectively separated from residual foam, and the cavitation of subsequent pipelines and fans can be reduced.
In an embodiment of the above-mentioned combined packed absorption tower of the present invention, the inner sidewall of the liquid-foam phase mixing zone is provided with a plurality of turns of cooling coils of the liquid-foam phase mixing zone.
In some embodiments of the present invention, the cooling medium that may be used in the liquid-foam mixed phase zone cooling coil may be water, air, or other common coolants.
In a specific embodiment of the above combined packed absorption tower of the present invention, the first mist generator and the second mist generator preferably employ a montmork kinetic wave nozzle, and the average diameter of the formed mist droplets is less than 0.2 mm. The fresh solvent or the lean solvent is respectively sent to the first fog drop generator and the second fog drop generator through a lean solution pipeline, the fresh solvent or the lean solvent is divided into three strands, two strands of fresh solvent or lean solvent enter the nozzle along the tangential direction, and one strand of fresh solvent or lean solvent enters the nozzle along the axial direction and is respectively contacted with the flue gas in a counter-current or co-current mode from top to bottom.
In addition, the first mist generator and the second mist generator may be ultrasonic atomizers or steam atomizers.
As a specific embodiment of the above combined packed absorption tower of the present invention, the cross section of the combined packed absorption tower may be any shape, such as circular, oval, rectangular, etc., and may be selected reasonably according to actual situations on site.
In the invention, the side walls of the spray reaction zone, the gas flow uniform distribution zone and the foam reaction zone can be called as tower walls.
In another aspect, the present invention provides a flue gas purification process, wherein the flue gas purification process utilizes the combined packed absorption tower described above, comprising:
(1) the flue gas enters the spraying reaction area from the gas inlet pipe and upwards passes through the packing layer, and is in countercurrent contact with semi-rich liquid sprayed by the liquid distributor in the packing layer, so that the flue gas is purified for one time;
(2) the flue gas which is subjected to the primary purification treatment in the step (1) enters a flue or a pipeline and continues to rise, and in the rising process, fine fog drops sprayed by the first fog drop generator are in contact with the flue gas and are subjected to cooling, dust removal and secondary purification treatment;
(3) the flue gas which completes the secondary purification treatment in the step (2) enters a foam reaction zone, and when the micro fog drops sprayed by the second fog drop generator pass through a plurality of micropore filler sections along with the flue gas flow, the gas flow is blocked by the fog drops to form dynamic foam and is contacted with the fog drops for mass transfer to form a mixture of micro drops and foam;
and then the mixture enters a liquid-foam mixed phase region along with the flue gas, the foam in the mixture forms semi-rich liquid under the action of quenching, and falls to a temporary liquid storage region, and finally the flue gas after the third purification treatment in a microporous filling section and the liquid-foam mixed phase region is discharged.
As a specific embodiment of the above process of the present invention, the process further comprises: after the liquid level in the temporary liquid storage area reaches a certain degree, the semi-rich liquid in the temporary liquid storage area is pressurized through the circulating pump and is sent to the liquid distributor through the return pipeline for spraying.
The purification process/principle of the purification process of the flue gas provided by the invention is as follows:
firstly, flue gas enters a spraying reaction area from an air inlet pipe and upwards passes through a packing layer, and is in countercurrent contact with semi-rich liquid sprayed by a liquid distributor in the packing layer so that the flue gas is purified for one time;
secondly, the flue gas which is subjected to the primary purification treatment in the previous step enters a flue or a pipeline and continues to rise, and in the rising process, the fine fog drops sprayed by the first fog drop generator are in contact with the flue gas to carry out cooling, dust removal and secondary purification treatment on the flue gas;
and thirdly, the flue gas which is subjected to secondary purification treatment in the previous step enters a foam reaction zone, the barren solution is dispersed at a certain divergence angle by the second fog drop generator through the nozzle to form uniform and fine fog drops, and when the fog drops pass through the pore channel of the microporous screen plate along with the air flow, the air flow is blocked by the fog drops to form dynamic foam with small diameter and severe disturbance. The two-phase mass transfer surface in the foam contact state is not a few bubble surfaces but a liquid film with a large area. This liquid film, unlike the stable foam formed by the presence of surfactants, is highly turbulent and will continually coalesce and break up, creating good hydrodynamic conditions for two-phase mass transfer. At the moment, the dynamic foam and the fog drops are contacted for mass transfer to form a mixture of micro-droplets and foam;
then the mixture enters a liquid-foam mixed phase region along with the flue gas, under the action of rapid cooling, foam in the mixture forms semi-rich liquid and falls to a temporary liquid storage region, and then the flue gas after the third purification treatment in a microporous filling section and the liquid-foam mixed phase region is discharged;
and finally, pressurizing the semi-rich liquid formed after the foam is broken, sending the semi-rich liquid to a liquid distributor through a return pipeline for spraying, and further finishing the purification of the acid gas through the secondary reaction of the semi-rich liquid and the acid gas contained in the flue gas in the packing layer, thereby finishing the absorption internal circulation of the acid gas contained in the flue gas.
Compared with the prior art, the beneficial technical effects which can be achieved by the invention comprise:
in the invention, foam is adopted to replace part of complex filler structures, the liquid-gas contact surface area is increased, mass transfer is accelerated, the reaction surface is continuously and violently broken and recombined to greatly improve the mass transfer efficiency, and meanwhile, a high concentration gradient can be generated in the process to maximize the mass transfer driving force.
In the invention, because the gas is in turbulent contact with the extremely large and rapidly renewed liquid surface to form a foam zone, the foam generation zone and the liquid-foam mixed phase zone are provided with heat exchange devices (cooling coils) to generate gas quenching effect, and the temperature reduction can improve the absorption of CO by the absorbent 2 Thereby improving CO mass transfer 2 The absorption capacity of the absorption tower is reduced.
In the invention, the flue gas is subjected to pre-spraying treatment in the rising process of the flue gas in the flue, when liquid drops are quickly evaporated, the concentration gradient of steam components is generated in the area near the liquid drops to form Stefin flow which flows and diffuses outwards from the liquid drops, and submicron and micron-sized impurity particles in the gas move under the conveying action of the Stefin flow and finally contact and adhere to condensed liquid drops to be wetted and trapped, so that the risk that the condensed liquid drops enter a subsequent microporous filler to block a pore plate is reduced.
In the invention, each micropore filling section comprises two layers of filling materials, namely an upper layer filling material and a lower layer filling material, and the pore diameter of each layer of filling material is different, so that the net passing air speed can be fully controlled. In addition, the liquid phase is in a moving foam state on the microporous packing, the air passing speed after passing through the orderly structured microporous mesh plate packing and the disordered porous silicon carbide packing is increased layer by layer, the transverse movement of the foam is greatly enhanced, the turbulence degree between the gas phase and the liquid phase on the surface of the foam is high, the contact area between the gas phase and the liquid phase is large, the gas phase and the liquid phase are continuously updated, and the mass transfer effect is continuously enhanced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a packed absorption tower according to embodiment 1 of the present invention.
FIG. 2 is a schematic structural diagram of any two adjacent microporous filler sections and the foam free mixing zone formed therebetween in example 1 of the present invention.
Fig. 3 is a schematic structural diagram of any microporous filler section in embodiment 1 of the present invention.
FIG. 4 is a schematic structural diagram of the upper layer filler in any microporous filler section in example 1 of the present invention.
FIG. 5 is a schematic structural diagram of the underfill material in any one of the microporous underfill material sections in example 1 of the present invention.
Fig. 6 is a schematic cross-sectional view of any one of the microporous filler sections in embodiment 1 of the present invention.
The main reference numbers illustrate:
10. an air inlet pipe; 100. an air inlet;
11. a liquid outlet;
12. a filler layer;
13. a liquid distributor;
14. a liquid storage area;
15. a baffle;
16. a first droplet generator; 160. a lean liquid line;
17. a rectifying grid;
18. a second droplet generator;
19. a liquid-foam phase mixing zone; 190. a liquid-foam mixed phase zone cooling coil;
20. a flue; 200. a tower wall; 201. a flue inlet; 202. a flue outlet;
21. an air outlet pipe; 210. a wire mesh demister;
22. a temporary liquid storage area; 220. a liquid discharge port;
23. a circulation pump; 230. a return line;
24. a microporous filler section; 240. filling the upper layer; 240a, micro-porous net plate structure meshes; 240b, a micro-porous net plate structure net plate; 241. lower layer filling; 241a, silicon carbide orifices; 241b, a silicon carbide mesh plate; 242. a foam generating area; 243. a venturi cooling coil; 244. a water-resistant material; 245. an overflow section; 246. a water retaining weir; 247. a foam free mixing zone; 248. a support bar;
25. a retractable nozzle; 250. a media line.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. The following described embodiments are some, but not all embodiments of the present invention, and are merely illustrative of the present invention and should not be construed as limiting the scope of the present invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
It should be noted that the term "comprises/comprising" and any variations thereof in the description and claims of this invention and the above-described drawings is intended to cover non-exclusive inclusions, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
In the present invention, the terms "upper", "lower", "inner", "outer", "middle", "top" and "bottom" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings. These terms are used primarily to better describe the invention and its embodiments and are not intended to limit the indicated devices, elements or components to a particular orientation or to be constructed and operated in a particular orientation.
Moreover, some of the above terms may be used to indicate other meanings besides the orientation or positional relationship, for example, the term "on" may also be used to indicate some kind of attachment or connection relationship in some cases. The specific meanings of these terms in the present invention can be understood by those skilled in the art as appropriate.
Furthermore, the terms "disposed" and "connected" should be interpreted broadly. For example, "connected" may be a fixed connection, a detachable connection, or a unitary construction; can be a mechanical connection, or an electrical connection; may be directly connected, or indirectly connected through intervening media, or may be in internal communication between two devices, elements or components. The specific meanings of the above terms in the present invention can be understood by those of ordinary skill in the art according to specific situations.
In the invention, the alcohol amine solution is a general name of a class of organic alkali solution, and generally refers to a weakly alkaline organic amine solvent used for absorbing hydrogen sulfide or carbon dioxide in a desulfurization and decarburization chemical process;
the rich solution is a solution (containing the absorbed component) flowing out from the bottom of the tower after the soluble component is absorbed by the absorbent in the tower in the absorption operation process of the absorption tower;
the semi-rich solution only absorbs part of CO 2 But not completely converted into a lean solution of a rich solution;
the lean solution is a solution which is separated from the absorbent into easily soluble components and flows out from the bottom of the column in the desorption operation of the desorption column.
The "ranges" disclosed herein are given as lower and upper limits. There may be one or more lower limits, and one or more upper limits, respectively. The given range is defined by the selection of a lower limit and an upper limit. The selected lower and upper limits define the boundaries of the particular range. All ranges defined in this manner are combinable, i.e., any lower limit can be combined with any upper limit to form a range. For example, ranges of 60-120 and 80-110 are listed for particular parameters, with the understanding that ranges of 60-110 and 80-120 are also contemplated. Further, if the minimum range values listed are 1 and 2 and the maximum range values listed are 3, 4, and 5, then the following ranges are all contemplated: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.
In the present invention, unless otherwise stated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, a numerical range of "0 to 5" indicates that all real numbers between "0 to 5" have been listed throughout this disclosure, and "0 to 5" is only a shorthand representation of the combination of these numbers.
In the present invention, all the embodiments and preferred embodiments mentioned in the present invention may be combined with each other to form a new technical solution, if not specifically stated.
In the present invention, all the technical features mentioned in the present invention and preferred features may be combined with each other to form a new technical solution, if not specifically stated.
Example 1
The embodiment provides a combined filler absorption tower, a schematic structural diagram of which is shown in fig. 1, and as can be seen from fig. 1, the combined filler absorption tower is of a single tower structure, a tower body of the combined filler absorption tower is a cylindrical and vertically extending tower body, and comprises a spraying reaction area, an air flow uniform distribution area and a foam reaction area, wherein the spraying reaction area is located at the bottom of the absorption tower, the air flow uniform distribution area and the foam reaction area are arranged at the upper part of the spraying reaction area side by side, and the bottom and the top of the air flow uniform distribution area are respectively communicated with the top of the spraying reaction area and the top of the foam reaction area;
the spraying reaction area is provided with a liquid storage area 14, an air inlet pipe 10, a packing layer 12 and a liquid distributor 13 from bottom to top, wherein a liquid outlet 11 is arranged on one side of the liquid storage area 14, and an air inlet 100 is arranged on one side of the air inlet pipe 10; the filler layer 12 is a stainless steel 316L plate corrugated structured filler with the model number of M250Y;
the airflow uniform distribution area comprises a flue 20 and a plurality of first fog drop generators 16 arranged at the top of the flue 20; a flow guide plate 15 is arranged on an elbow at the top of the flue 20, a flue inlet at the top of the foam reaction zone/a flue outlet at the top of the airflow uniform distribution zone 202 is of a triangular wing structure, a layer of rectifying grating 17 is arranged at the intersection of the triangular wing structure and the tower wall 200, a flue inlet 201 at the intersection of the bottom of the flue and the spray reaction zone is of a triangular structure, and the oblique side of the triangular structure is connected with the tower wall 200 on the opposite side of the flue;
the foam reaction zone is provided with a second fog drop generator 18, a micropore filling section 24, a liquid-foam mixed phase zone 19, an air outlet pipe 21 and a temporary liquid storage zone 22 from top to bottom; the second fog drop generator 18 is arranged below the rectification grille 17, and the barren solution pipeline is respectively communicated with the first fog drop generators 16 and the second fog drop generators 18; the air inlet end of the air outlet pipe 21 faces downwards and is provided with a wire mesh demister 210, and the diameter of an orifice of the wire mesh demister 210 is 3 mm; a liquid outlet 220 is formed in one side of the temporary liquid storage region 22, and the liquid outlet 220 is communicated with the liquid distributor 13 through a return pipeline 230 via a circulating pump 23; the inner side wall of the liquid-foam mixed phase region 19 is provided with a plurality of circles of liquid-foam mixed phase region cooling coils 190;
in this embodiment, the number of the microporous filler sections 24 is 3, a foam free mixing area 247 is formed between adjacent microporous filler sections 24, and a schematic structural diagram of any two adjacent microporous filler sections 24 and the foam free mixing area 247 formed therebetween is shown in fig. 2;
the schematic structural diagram of any microporous filler section 24 is shown in fig. 3, and as can be seen from fig. 3, the microporous filler section 24 includes an upper layer of filler 240, a lower layer of filler 241, and a foam generation region 242 formed between the upper layer of filler 240 and the lower layer of filler 241, where the schematic structural diagrams of the upper layer of filler 240 and the lower layer of filler 241 are respectively shown in fig. 4, fig. 5, and fig. 6, the upper layer of filler 240 is an ordered and regular microporous mesh plate structured filler, the lower layer of filler 241 is an unordered porous silicon carbide filler, and the pore diameters of the upper layer of filler 240 and the pore diameter of the lower layer of filler 241 are different; specifically, in this embodiment, the upper layer filler 240 is a U-shaped microporous mesh plate structured filler, and on the wave crest, the wave trough and the side wall plate, that is, the microporous mesh plate structured mesh 240b is uniformly distributed with microporous mesh plate structured meshes 240a with a diameter of 0.04mm, and the lower layer filler 241 is a non-metal porous foam silicon carbide filler with a diameter (that is, the diameter of the silicon carbide orifice 241a, the silicon carbide orifice 241a being opened in the silicon carbide mesh plate 241b) of 1.5 mm;
the froth generation zone 242 has a venturi structure with multiple turns of venturi cooling coil 243 wound from top to bottom outside the venturi structure;
the upper-layer packing 240 and the lower-layer packing 241 respectively comprise a grid support structure formed by support rods 248, a circular packing ring is arranged in each grid, the packing, namely a U-shaped microporous mesh plate structure packing and a non-metal porous foam silicon carbide packing, is filled in the circular packing ring, and the water-resistant material 244 is filled in the gap between each grid and the circular packing ring and the gap between each support rod 248 and the tower wall 200 (see four corners shown by arrows in fig. 6) where no grid is formed; the upper-layer packing 240 and the lower-layer packing 241 are respectively provided with 32 circular packing rings, and the water-resistant material 244, the support rod 248, the circular packing rings, the water-retaining weir 246, the tower wall and the like are all made of 316L stainless steel;
the number of the second fog drop generators 18 is the same as that of the circular packing rings, and the centers of the nozzles of the second fog drop generators 18 are opposite to the centers of the circular packing rings;
wherein, the outer side of the microporous filler section 24 is provided with a water-retaining weir 246, the side of the water-retaining weir 246 facing the microporous filler section 24 is respectively connected with the upper layer filler 240 and the lower layer filler 241, the upper end of the water-retaining weir 246 is slightly higher than the upper layer filler 240, the side of the water-retaining weir 246 facing away from the microporous filler section 24 is connected with the inner side wall of the foam reaction zone through a horizontal connecting section, and an overflow section 245 is formed between the side of the water-retaining weir 246 facing away from the microporous filler section 24 and the inner side wall of the foam reaction zone;
in this embodiment, the horizontal connecting section is also composed of a microporous filler, and the material of the horizontal connecting section is consistent with that of the filler on the upper layer, namely the horizontal connecting section is made of a filler with a U-shaped microporous reticular plate structure; and the side/vertical surface of the water-retaining weir 246 opposite to the microporous filler section 24 is connected with the inner side wall of the foam reaction zone through two horizontal connecting sections which are parallel to each other and are respectively positioned at the same height with the upper layer filler 240 and the lower layer filler 241;
wherein, a plurality of retractable nozzles 25 are arranged below the lower layer filler 241 and can be retracted to the edge of the tower wall 200, and the plurality of retractable nozzles 25 are communicated with the medium pipeline 250.
In this embodiment, the first mist generator 16 and the second mist generator 18 are implemented by a montgomo kinetic wave nozzle, and the average diameter of the formed mist drops is less than 0.2 mm. Fresh or lean solvent is fed through the lean liquid line to the first and second mist generators 16 and 18, respectively, and the fresh or lean solvent is split into three streams, two of which enter the nozzle tangentially and one of which enter the nozzle axially and are contacted with the flue gas in a counter-current or co-current manner from top to bottom, respectively.
Example 2
The embodiment provides a flue gas purification process, wherein the flue gas purification process utilizes the combined packed absorption tower provided in embodiment 1, and comprises the following specific steps:
removing impurities from flue gas from power plant after desulfurization and denitration, wherein the temperature of the obtained flue gas is 40 ℃, and the flue gas contains 12% vol CO 2 And the remainder of N 2 When the flue gas is non-acidic gas, the flue gas enters the spraying reaction area from the gas inlet of the gas inlet pipe and moves upwards to pass through the packing layer, and the flue gas is in countercurrent contact with semi-rich liquid sprayed by the liquid distributor in the packing layer, so that the flue gas is purified for the first time, the semi-rich liquid in countercurrent contact with the flue gas is changed into rich liquid to be collected in the liquid storage area, and the rich liquid is discharged from the liquid outlet of the liquid storage area;
the flue gas after primary purification treatment continuously rises along the flue through a flue inlet with a triangular structure, and in the rising process, a spray head of a first fog drop generator at the top of the flue starts spraying to generate fine fog drops which are in countercurrent contact with the flue gas, so that the flue gas is subjected to cooling, dust removal and secondary purification treatment;
the flue gas after the secondary purification treatment enters a foam reaction area under the drainage action of a guide plate and a rectifying grid, liquid sprayed out of a spray head of a second droplet generator is uniformly and radially diffused, and after passing through an upper layer of filler, a plurality of bubbles with the diameter of 3-5 mm are generated, a cavity of a foam generation area is sealed from the middle to the outside, so that the liquid rotates and overturns on the microcosmic and is in strong turbulent impact contact with gas, the surface updating capability is improved, a dynamically balanced foam area is established, the cavity of the foam generation area is of a Venturi tube structure, the downward migration of foam can be accelerated, the resistance formed by the foam is offset, a foam free mixing area is arranged between adjacent microporous filler sections, in the area, the foam, micro-droplets and broken bubbles are in disordered contact, are violently broken and recombined, a mixture of the micro-droplets and the foam is formed again, and simultaneously flows to the next microporous filler section under the inertia action of the flue gas, repeating the above steps until all the microporous filler sections are passed;
under the condition that the liquid-gas ratio L/G is 4, 65-90% of absorption process occurs in the atomizing and foaming stages, the droplet size is controlled to be less than 100 μm, and the average foam diameter can be controlled to be 3-3.7 mm; compared with the technology of flue gas purification by only adopting an absorption tower filled with 250Y regular packing in the prior art, the flue gas purification method adopts the combination of fine spray and foam to purify the flue gas, so that the gas-liquid contact specific surface area can be improved by 6 times, and the absorption rate can be improved by 4 times;
fresh solvent or lean solvent is respectively sent to a first fog drop generator and a second first fog drop generator through a lean solution pipeline, and is sprayed out by a spray nozzle to form fine fog drops which react with flue gas;
the reaction of absorbing acid gas by an absorbent (the absorbent used in the embodiment is an aqueous solution of MEA with a mass concentration of 30%) is an exothermic reaction, the temperature rise in the reaction process is not beneficial to the reaction, a venturi cooling coil is arranged around a venturi tube wall plate of a cavity of a foam generation area, flue gas, foam and fog drops are cooled (to 7 ℃) under the heat exchange action of a cooling medium such as water, air or other common coolants, the foam is accelerated to crack and recombine under the action of rapid cooling, the liquid-gas contact frequency is increased, and the mass transfer capacity is improved;
the flue gas enters a liquid-foam mixed phase region after passing through all the micropore filler sections, the tower wall of the region is provided with a plurality of circles of liquid-foam mixed phase region cooling coils, and the used cooling medium can also be water, air or other common cooling agents and the like; losing the secondary generating acting force in the area, rapidly breaking the foam under the action of rapid cooling (cooling to 12 ℃), converging the foam into small liquid drops, further polymerizing the small liquid drops into larger liquid drops, forming semi-rich liquid and dropping the semi-rich liquid into a temporary liquid storage area, starting a circulating pump after the liquid level of the temporary liquid storage area reaches a certain degree, pressurizing the semi-rich liquid and then sending the semi-rich liquid to a liquid distributor through a return pipeline for spraying, thereby completing the absorption internal circulation of the acid gas contained in the flue gas. The flue gas is purified for the third time in the micropore filling section and the liquid-foam mixed phase area, the purified flue gas is discharged through the gas outlet pipe, and residual CO in the purified flue gas 2 To a volume concentration of 1% vol, CO 2 The removal rate of the catalyst reaches more than 90 percent.
The air inlet end of the air outlet pipe faces downwards and is provided with a silk screen demister, so that the purified gas of the foam layer can be effectively separated from residual foam, and cavitation of subsequent pipelines and fans is reduced;
after a period of operation, the filler in the microporous filler section can be blocked, so that the pressure drop in the tower is overlarge, at the moment, the telescopic spray head arranged below the lower-layer filler is started, the filler is simply and quickly swept, and the blockage of the filler hole is dredged under the action of compressed air or superheated steam.
In conclusion, in the embodiment of the invention, foam is adopted to replace part of a complex filler structure, the liquid-gas contact surface area is increased, the mass transfer is accelerated, the reaction surface is continuously and violently broken and recombined to greatly improve the mass transfer efficiency, and meanwhile, a high concentration gradient can be generated in the process to maximize the mass transfer driving force.
In the embodiment of the invention, because the gas is in turbulent contact with the extremely large and rapidly renewed liquid surface to form a foam area, the foam generation area and the liquid-foam mixed phase area are provided with heat exchange devices (cooling coils) to generate gas quenching effect, and the temperature reduction can improve the absorption of CO into the absorbent 2 Thereby improving CO mass transfer 2 The absorption capacity of the absorption tower is reduced.
In the embodiment of the invention, the flue gas is subjected to pre-spraying treatment in the rising process in the flue, when liquid drops are quickly evaporated, the concentration gradient of steam components is generated in the area near the liquid drops to form Stefin flow diffused from the liquid drops to the outside, submicron and micron-sized impurity particles in the gas move under the conveying action of the Stefin flow and finally contact and adhere to condensed liquid drops to be wetted and trapped, and the risk that the impurity particles enter a subsequent microporous filler to block a pore plate is reduced.
In the embodiment of the invention, each microporous filler section comprises two layers of fillers, namely an upper layer of filler and a lower layer of filler, and the pore diameter of each layer of filler is different, so that the air speed of passing through the net can be fully controlled. In addition, the liquid phase is in a moving foam state on the microporous filler, the air passing speed after passing through the ordered and regular microporous mesh plate filler and the disordered porous silicon carbide filler is increased layer by layer, the transverse movement of the foam is greatly enhanced, the turbulence degree between the gas phase and the liquid phase on the surface of the foam is high, the contact area between the gas phase and the liquid phase is large, the gas phase and the liquid phase are continuously updated, and the mass transfer effect is continuously enhanced.
The above description is only exemplary of the invention and should not be taken as limiting the scope of the invention, so that the invention is intended to cover all modifications and equivalents of the embodiments described herein. In addition, the technical features and the technical inventions of the present invention, the technical features and the technical inventions, and the technical inventions can be freely combined and used.

Claims (15)

1. The combined type packing absorption tower is characterized by comprising a single tower structure or a double tower structure, and when the combined type packing absorption tower is of the single tower structure, the combined type packing absorption tower comprises a spraying reaction area, an air flow uniform distribution area and a foam reaction area, wherein the spraying reaction area is positioned at the bottom of an absorption tower, the air flow uniform distribution area and the foam reaction area are arranged at the upper part of the spraying reaction area side by side, and the bottom and the top of the air flow uniform distribution area are respectively communicated with the top of the spraying reaction area and the top of the foam reaction area;
the spraying reaction area is provided with a liquid storage area, an air inlet pipe, a packing layer and a liquid distributor from bottom to top, the air flow uniform distribution area comprises a flue and a first fog drop generator arranged at the top of the flue, and the foam reaction area is provided with a second fog drop generator, a plurality of micropore filling sections, a liquid-foam mixed phase area, an air outlet pipe and a temporary liquid storage area from top to bottom;
when the double-tower structure is adopted, the double-tower structure comprises a first absorption tower and a second absorption tower, wherein the first absorption tower is communicated with the second absorption tower through a pipeline, a liquid storage area, an air inlet pipe, a packing layer and a liquid distributor are arranged in the first absorption tower from bottom to top, and a second fog drop generator, a plurality of micropore packing sections, a liquid-foam mixed phase area, an air outlet pipe and a temporary liquid storage area are arranged in the second absorption tower from top to bottom.
2. The integrated, packed absorption column of claim 1, wherein the liquid discharge of the temporary storage area communicates with the liquid distributor via a recirculation pump via a return line.
3. The modular packed absorption tower of claim 1 or 2, wherein the flue inlet at the intersection of the bottom of the flue and the spray reaction zone is of a right triangle configuration, and the hypotenuse of the right triangle configuration is connected to the tower wall on the opposite side of the flue.
4. The modular packing absorption tower of claim 1 or 2, wherein the flue inlet at the joint of the top of the flue and the foam reaction zone is further provided with a flow guide plate and a flow straightening grid respectively for guiding the gas in the flue to the foam reaction zone.
5. The modular packing absorption tower of claim 1, wherein the plurality of microporous packing segments comprise an upper packing, a lower packing and a foam generation zone formed between the upper packing and the lower packing, wherein the upper packing is an ordered and regular microporous mesh plate structured packing, the lower packing is a disordered porous silicon carbide packing, and the pore diameters of the upper packing and the lower packing are different.
6. The combined packing absorption tower of claim 5, wherein the upper layer of packing is U-shaped micro-porous reticular plate structured packing, meshes with diameters smaller than 0.05mm are uniformly distributed on the wave crests, the wave troughs and the side wall plates, and the lower layer of packing is non-metal porous foam silicon carbide packing with the diameter of 1-2 mm.
7. The combined packing absorption tower according to claim 5 or 6, wherein the upper and lower packing layers respectively comprise a grid support structure formed by support rods, each grid is internally provided with a circular packing ring, the packing is filled in the circular packing ring, and a gap between the grid and the circular packing ring is filled with a water-resistant material;
the number of the second fog drop generators is the same as that of the circular packing rings, and the centers of the nozzles of the second fog drop generators are opposite to the centers of the circular packing rings.
8. The combined packing absorption tower according to claim 5 or 6, wherein a water-retaining weir is disposed at the outer side of the microcellular packing section, the side of the water-retaining weir facing the microcellular packing section is respectively connected with the upper layer of packing and the lower layer of packing, the upper end of the water-retaining weir is higher than the upper layer of packing, the side of the water-retaining weir facing away from the microcellular packing section is connected with the inner sidewall of the foam reaction zone through a horizontal connection section, and an overflow section is formed between the side of the water-retaining weir facing away from the microcellular packing section and the inner sidewall of the foam reaction zone.
9. The modular packed absorption tower of claim 5 or 6, wherein the foam generation zone has a venturi structure.
10. The modular packing absorption tower of claim 9, wherein the venturi structure is wrapped with a plurality of turns of cooling coil from top to bottom.
11. The combined packing absorption tower according to claim 1 or 2, wherein the number of the microporous packing sections is n +1, wherein n is an integer not less than 1;
and a foam free mixing area is formed between the adjacent microporous filler sections.
12. The combined packing absorption tower of claim 5 or 6, wherein a plurality of retractable spray heads are arranged below the lower packing and can be retracted to the edge of the tower wall.
13. The modular packed absorption tower of claim 1 or 2, wherein the inlet end of the outlet pipe is directed downward and is provided with a wire mesh demister.
14. The modular packed absorption column of claim 1 or 2, wherein the inner side wall of the liquid-foam phase mixing zone is provided with a plurality of turns of cooling coils.
15. A flue gas purification process using the modular packed absorption tower of any one of claims 1-14, comprising:
(1) the flue gas enters the spraying reaction area from the gas inlet pipe and upwards passes through the packing layer, and is in countercurrent contact with semi-rich liquid sprayed by the liquid distributor in the packing layer, so that the flue gas is purified for one time;
(2) the flue gas which is subjected to the primary purification treatment in the step (1) enters a flue or a pipeline and continues to rise, and in the rising process, fine fog drops sprayed by the first fog drop generator are in contact with the flue gas and are subjected to cooling, dust removal and secondary purification treatment;
(3) the flue gas which completes the secondary purification treatment in the step (2) enters a foam reaction zone, and when the micro fog drops sprayed by the second fog drop generator pass through a plurality of micropore filler sections along with the flue gas flow, the gas flow is blocked by the fog drops to form dynamic foam and is contacted with the fog drops for mass transfer to form a mixture of micro drops and foam;
and then the mixture enters a liquid-foam mixed phase region along with the flue gas, the foam in the mixture forms semi-rich liquid under the action of quenching, and falls to a temporary liquid storage region, and finally the flue gas after the third purification treatment in a microporous filling section and the liquid-foam mixed phase region is discharged.
CN202210739769.XA 2022-06-28 2022-06-28 Combined packing absorption tower and flue gas purification process Pending CN114904369A (en)

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CN202210739769.XA CN114904369A (en) 2022-06-28 2022-06-28 Combined packing absorption tower and flue gas purification process

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CN114904369A true CN114904369A (en) 2022-08-16

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