CN112221286A - Deep absorption tower for flue gas treatment, flue gas treatment system and process - Google Patents
Deep absorption tower for flue gas treatment, flue gas treatment system and process Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
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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
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- 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
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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Abstract
The invention relates to a deep absorption tower, a system and a process for flue gas treatment, wherein the deep absorption tower, the system and the process can be suitable for large-range working condition fluctuation of flue gas and have wide adaptability; the deep dedusting and demisting device adopts the atomizing nozzle, forms large-particle-size micro-clusters through collision, and is combined with the secondary dedusting and demisting device for application, so that the cost of deep dedusting and demisting is reduced; the water spray and water curtain spray sections adopt overflow pipes controlled by liquid levels, so that the complexity of system control is reduced; the flue gas condensation is arranged at the downstream of the main absorption process, and two-stage cooling of a tube type heat exchanger, a wound tube type heat exchanger or a plate type heat exchanger is adopted, so that not only is the blockage of a cooler avoided, but also the heat exchange efficiency is greatly improved, the equipment specification is reduced, meanwhile, the cooling medium adopts industrial circulating water to meet the flue gas condensation requirement, and no additional cold source is required; the flue gas condensation setting greatly reduces the consumption of system make-up water.
Description
Technical Field
The invention relates to a flue gas purification process, in particular to a deep absorption tower for deep desulfurization and dust removal of flue gas, a flue gas treatment system and a flue gas treatment process.
Background
In recent years, along with the increasing severity of environmental problems, the nation has paid more attention to environmental protection problems, and the emission standard of atmospheric pollution areas is continuously improved. In order to meet the increasingly stringent requirements of pollutant emission standards, various subsequent treatment technologies for discharged flue gas in industrial production need to be continuously perfected and improved.
Atmospheric pollution refers to the condition that certain substances enter the atmosphere due to human activities or natural processes, present sufficient concentration and last for a certain time, and reach the degree of harming human health and environment. Among them, sulfides, dust, fly ash, liquid droplets, smoke, etc. are important components of air pollution, and how to purify sulfides in flue gas and eliminate particulate matters and smoke in discharged flue gas, even micron-sized and submicron-sized particulate matters, so as to meet the environmental protection requirements, becomes one of the key points of people in the technical field of flue gas desulfurization, dust removal and demisting.
The flue gas discharged by the petroleum refining industry occupies a large proportion of the emission of atmospheric pollutants, wherein the flue gas discharged by the regenerator of the catalytic cracking unit is the largest air pollution source of a refinery, and the flue gas comprises particulate matters, sulfur oxides, nitrogen oxides, carbon monoxide and the like. The regenerated flue gas from catalytic cracking has the characteristics of wide fluctuation range of sulfur content, large particle size range of particles, high content of particles below submicron level and the like.
Traditional flue gas desulfurization dust removal defogging technique lacks the research and the configuration of system, and is low to submicron order particulate matter treatment effeciency, along with the change of flue gas operating mode or the increase of submicron order particulate matter content in the flue gas, often can lead to desulfurization dust removal defogging efficiency to have satisfied the index requirement. For example, in the flue gas desulfurization system and the flue gas desulfurization method using the flue gas desulfurization system disclosed in the chinese patent application with publication number CN108079762A, flue gas directly enters the flue gas heat exchanger without being dedusted, which easily causes the blockage of the flue gas heat exchanger and the increase of energy consumption of the device or even the shutdown; the flue gas directly contacts with a large amount of quenching circulating liquid, and the drastic change of the operation condition causes the great fluctuation of the desulfurization efficiency, thereby being not beneficial to the standard-reaching emission of the flue gas; after being chilled, the flue gas horizontally enters a desulfurizing tower, so that the accumulation and hardening of particles in the flue gas in a horizontal section are easily caused; meanwhile, the flue gas desulfurization system is only provided with a layer of demister, particulate matters in the flue gas cannot be effectively absorbed, and particulate matters with particle sizes of submicron and below cannot be trapped.
Disclosure of Invention
The first technical problem to be solved by the invention is to provide a deep absorption tower for flue gas treatment, which has a good flue gas purification effect and is wide in sulfur content fluctuation range and large in particle size range, aiming at the current situation of the prior art.
The second technical problem to be solved by the invention is to provide a flue gas treatment system using the deep absorption tower, aiming at the current situation of the prior art, the system can adapt to a wide range of flue gas desulfurization and deep dedusting and demisting processes, and the flue gas purification effect is good.
The third technical problem to be solved by the present invention is to provide a flue gas treatment process of the flue gas treatment system, aiming at the current situation of the prior art.
The technical scheme adopted by the invention for solving at least one technical problem is as follows: the utility model provides a flue gas is handled with degree of depth absorption tower, includes the tower body, its characterized in that: the device comprises a water curtain spraying section, a primary dedusting and demisting section, a water mist spraying section and a secondary dedusting and demisting section which are sequentially arranged from bottom to top, wherein the bottom of a tower body is a liquid collection tower kettle, and the top of the tower body is provided with a flue gas outlet;
the side part of the tower body is provided with a flue gas inlet which is positioned above the tower kettle and below the water curtain spraying section, and the flue gas inlet and the axis of the tower body form an angle of 40-60 degrees;
the bottom of the water curtain spraying section is provided with a first liquid collecting tank capable of separating the water curtain spraying section from a lower area, the water curtain spraying section is provided with a gas lifting hole which vertically extends through the bottom wall of the first liquid collecting tank, and gas below the first liquid collecting tank enters the water curtain spraying section upwards along the gas lifting hole; the top of the water curtain spraying section is provided with water curtain nozzles arranged corresponding to the gas lifting holes;
a second liquid collecting groove capable of separating the water mist spraying section from a water curtain spraying section below the water mist spraying section is formed at the bottom of the water mist spraying section, a gas riser which vertically extends through the bottom wall of the second liquid collecting groove is arranged on the water mist spraying section, gas below the second liquid collecting groove enters the water mist spraying section upwards along the gas riser, the cross section area of the gas riser is larger than that of the gas riser, and an umbrella-shaped cover cap with an upward pointed end is covered above the gas riser; and the water mist spraying section is filled with filler positioned above the gas rising pipe, and a water mist nozzle is arranged above the filler.
Preferably, the gas lift hole be a plurality of and around the tower body center periphery be the shape of returning and arrange, gas lift hole top is provided with horizontal and three cascade absorption liquid distribution pipes that arrange side by side, the rivers nozzle locate on the cascade absorption liquid distribution pipe and with gas lift hole one-to-one, form the cascade that can cover gas lift hole upper end mouth at gas lift hole top. The structure is favorable for improving the flue gas purification effect.
Preferably, the cascade sprays the section and is provided with the overflow pipe that can lead to the column bottom with the hydrops of first catch basin, and this overflow pipe upper portion is provided with the horn mouth, and the upper end cross sectional area of this horn mouth is hypomere cross sectional area 1.5 times, and this overflow pipe lower part extends to main column bottom.
Preferably, the air risers are rectangular, and the six air risers are arranged in two rows; three transverse water-washing absorption liquid distribution pipes which are arranged side by side are arranged above the gas rising pipe, and the water mist nozzles are arranged on the water-washing absorption liquid distribution pipes.
Further preferably, washing absorbing liquid distributing pipe length in the middle of is greater than the washing absorbing liquid distributing pipe length of both sides, and the washing absorbing liquid distributing pipe that is located in the middle of is linked together through the catheter and the washing absorbing liquid distributing pipe that is located both sides respectively, the water smoke nozzle is a plurality of and connects respectively on the washing absorbing liquid distributing pipe, and each washing absorbing liquid distributing pipe arranges jointly and is two annular spraying area that the overcoat was put.
The utility model provides an use flue gas processing system who has above-mentioned flue gas to handle with degree of depth absorption tower which characterized in that: the deep absorption tower is characterized by comprising a main absorption tower and the deep absorption tower, wherein the main absorption tower is arranged at the upstream of the deep absorption tower and is used for chilling flue gas and capturing and reacting particles in the flue gas to absorb, a flue gas inlet of the deep absorption tower is connected with the output end of the main absorption tower, and a flue gas heater capable of heating the flue gas to the required temperature according to the configuration of the deep absorption tower is arranged at a flue gas outlet of the deep absorption tower.
Preferably, the main absorption tower is provided with an upper part and a lower part which are communicated with each other, the upper part is used for chilling the flue gas, and the lower part is provided with a large-caliber nozzle to form a foam zone which can be in turbulent contact with the flue gas and is used for trapping and reacting and absorbing particles in the flue gas.
A flue gas treatment process using the flue gas treatment system is characterized by comprising the following steps:
the temperature of the discharged flue gas sent from the battery compartment is 150-300 ℃, the discharged flue gas firstly enters the main absorption tower, and the circulating absorption liquid from the absorption tower circulating pump forms a layer of liquid film on the inner wall of the upper part of the main absorption tower, so that the influence of the high-temperature flue gas on the main absorption tower is avoided, and the flue gas is chilled. The flue gas then enters the lower part of the main absorption tower, the circulating absorption liquid is reversely sprayed out from the lower part of the main absorption tower through a large-caliber nozzle relative to the flue gas, a foam zone is formed at the lower tower of the main absorption tower, the flue gas reversely passes through the foam zone and collides with gas-liquid phase micro-clusters in the circulating absorption liquid, and therefore most of SO in the flue gas is enabled to be2And the particles are enriched in the circulating absorption liquid. The saturated flue gas discharged from the main absorption tower has the temperature of 50-80 ℃, the flue gas and the circulating absorption liquid enter the deep absorption tower through a connecting section in an inclined mode, the flue gas flows from bottom to top along the deep absorption tower, the circulating absorption liquid enters the tower kettle of the deep absorption tower and is pressurized to 0.3-1.0 Mpa (g) through a circulating pump of the absorption tower, the flue gas is divided into three strands, one strand is sent to the upper part of the main absorption tower to serve as chilling absorption liquid, the other strand is sent to the lower part of the main absorption tower to serve as main circulating absorption liquid, and the third strand is sent out of a boundary zone to serve as discharged wastewater, so that the situation that the enrichment of sulfate and particles in the. The mass flow ratio of the chilling absorption liquid, the main circulation absorption liquid and the discharged wastewater is 1 (10-100): 1, and the mass flow ratio is correspondingly adjusted according to factors such as the temperature of the flue gas, the dust content in the flue gas and the like.
Flue gas enters a water curtain spraying section through the arranged water curtain spraying section air lifting holes in the deep absorption tower, a water curtain nozzle is arranged above each air lifting hole in the water curtain spraying section, cooled water curtain absorption liquid forms a complete water film above each air lifting hole through the water curtain nozzle, the flue gas penetrates out of the water film and is subjected to heat transfer with the water curtain absorption liquid to be cooled to 47-57 ℃, and SO in the flue gas is further eliminated2Medicinal granulesSending the particles and entrained foam to a first-stage dust and mist eliminator, sending absorption liquid pumped out from the bottom of a water curtain absorption section to a water curtain circulating pump, pressurizing to 0.3-1.0 Mpa (g), cooling to 45-55 ℃ by a water curtain absorption liquid cooler, and sending to a water curtain nozzle; the water curtain absorption liquid cooler is a tube type heat exchanger.
The flue gas passes through a first-stage dust removal demister, particles above micron level and foams in the flue gas are removed, and then the flue gas enters a water mist spraying section through a gas lifting hole of the water mist spraying section. The water mist spraying section is provided with an atomizing nozzle, the cooled water mist absorption liquid forms mist drops with the particle size of about 100-500 mu m in the water mist spraying section through the atomizing nozzle, when the flue gas passes through the water mist spraying section, on one hand, the flue gas is in heat transfer with the water mist absorption liquid and cooled to 42-52 ℃, on the other hand, submicron particles in the flue gas continuously collide with the atomized absorption liquid to form large-particle-size micro-clusters which are adsorbed and dissolved in the water mist absorption liquid, meanwhile, SO2 in the flue gas is further eliminated, then the flue gas enters a secondary dust removal demister, the absorption liquid extracted from the bottom of the water mist spraying section is sent to a water mist circulating pump to be pressurized to 0.3-1.0 Mpa (g), and then the absorption liquid is sent to the water mist nozzle after being cooled to. The water mist absorption liquid cooler is a plate type heat exchanger or a wound tube type heat exchanger.
The flue gas passes through a secondary dust and mist removing device to further remove large-particle-size micro-aggregates formed in the water mist spraying section and water mist carried in the flue gas, and the flue gas is heated by a flue gas heater and then sent out of a boundary region, and SO in the flue gas2The content is controlled at 5mg/Nm3The content of the particulate matters is controlled within 5mg/Nm3Within.
The flue gas heater is a high-efficiency wound pipe type heat exchanger, and steam heating, hot water heating or other heating media are selected according to the configuration of a factory device.
And (4) sending the make-up water from the battery limits to a water mist spraying section of the deep absorption tower to be used as system make-up water.
And the alkali liquor from the battery limits is respectively sent to suction inlet pipelines of the absorption tower circulating pump, the water curtain circulating pump and the water mist circulating pump.
Preferably, the flow of the alkaline solution sent to the inlet of the circulating pump of the absorption tower is adjusted, and the pH value of the circulating absorption solution is controlled to be 5-9. And adjusting the flow of the alkaline liquid sent to the inlet of the water curtain circulating pump, and controlling the pH value of the water curtain absorption liquid to be 6-10. And adjusting the flow of the alkaline liquid sent to the inlet of the water mist circulating pump, and controlling the pH value of the water mist absorption liquid to be 6-10.
In order to avoid the enrichment of particles and sulfate in the water mist absorption liquid, the water mist spraying section is provided with an overflow pipeline which automatically flows to the water curtain spraying section; in order to avoid the enrichment of particles and sulfate in the water curtain absorption liquid, the water curtain spraying section is provided with an overflow pipeline which automatically flows to the tower kettle of the deep absorption tower.
Preferably, soluble salts (as SO) in the circulating absorption liquid are controlled4 2-Calculated) the content is lower than 6-10 wt%, and the concentration of the particles is lower than 3-5 g/L.
Preferably, the concentration ratio of the particulate matters in the circulating absorption liquid, the water curtain absorption liquid and the water mist absorption liquid is controlled to be (100-400): (10-20): 1.
Compared with the prior art, the invention has the advantages that: the deep absorption tower, the flue gas treatment system and the process can be suitable for large-range working condition fluctuation of flue gas, and have wide adaptability; the deep dedusting and demisting device adopts the atomizing nozzle, forms large-particle-size micro-clusters through collision, and is combined with the secondary dedusting and demisting device for application, so that the cost of deep dedusting and demisting is reduced; the water spray and water curtain spray sections adopt overflow pipes controlled by liquid levels, so that the complexity of system control is reduced; the flue gas condensation is arranged at the downstream of the main absorption process, and two-stage cooling of a tube type heat exchanger, a wound tube type heat exchanger or a plate type heat exchanger is adopted, so that not only is the blockage of a cooler avoided, but also the heat exchange efficiency is greatly improved, the equipment specification is reduced, meanwhile, the cooling medium adopts industrial circulating water to meet the flue gas condensation requirement, and no additional cold source is required; the flue gas condensation setting greatly reduces the consumption of system make-up water.
Drawings
FIG. 1 is a schematic structural view of a deep absorption tower according to an embodiment of the present invention;
FIG. 2 is a diagram illustrating the arrangement of the spray section of the water curtain according to the embodiment of the present invention;
FIG. 3 is a diagram of the arrangement of the gas rising holes of the water mist spraying section according to the embodiment of the invention;
FIG. 4 is a diagram of a water mist spray nozzle of the water mist spray section according to an embodiment of the invention;
FIG. 5 is a process flow diagram of a flue gas treatment system according to an embodiment of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 4, the deep absorption tower 1 of the present embodiment includes a flue gas inlet 11, a water curtain spraying section 12, a first-stage dust and mist eliminator 13, a water mist spraying section 14, a second-stage dust and mist eliminator 15, a flue gas outlet 16, a water mist spraying section overflow pipe 17, a water curtain water mist spraying section overflow pipe 18, and a tower kettle 19. The water curtain spraying section 12, the primary dust-removing demister 13, the water mist spraying section 14 and the secondary dust-removing demister 15 are arranged from bottom to top, and correspondingly, flue gas flows from bottom to top after entering the tower body from the flue gas inlet 11.
The flue gas inlet 11 is arranged at the lower part of the deep absorption tower 1, and forms an included angle a of 45 degrees with the tower body;
the lower part of the water curtain spraying section 12 is provided with a water curtain spraying section air lifting hole 121 and a water curtain absorption liquid extraction port 124, and the upper part of the water curtain spraying section 12 is provided with a water curtain absorption liquid distribution pipe 122 and a water curtain nozzle 123;
the water curtain absorption liquid distribution pipes 122 are connected with the tower body through flanges, and the number of the water curtain absorption liquid distribution pipes is three;
the water curtain nozzles 123 correspond to the water curtain spraying section air lifting holes 121 one by one, and the water curtain nozzles 123 and the water curtain spraying section air lifting holes 121 are arranged in a rectangular shape in the tower body;
the water curtain spraying section 12 is provided with an overflow pipe 18, the upper part of the overflow pipe 18 is provided with a bell mouth, the sectional area of the upper end of the bell mouth is 1.5 times of that of the lower section, and the lower part is provided with an extension pipe which extends to the lower part of a tower kettle 19 of the main absorption tower;
the upper part of the water curtain spraying section 12 is provided with a primary dust and mist removing device 13;
the upper part of the first-stage dust and mist removing device 13 is provided with a water mist spraying section 14, the lower part of the water mist spraying section 14 is provided with a water mist spraying section riser 141, a water mist absorption liquid extraction outlet 145 and a water replenishing port 144, the middle part is provided with a packing layer 142, and the upper part is provided with a water mist absorption liquid distribution pipe 143 and a water mist nozzle 144;
the water mist spraying section riser 141 is rectangular and is uniformly arranged in the tower body 1;
the water mist absorption liquid distribution pipes 143 are connected with the tower body 1 through flanges, and the number of the water mist absorption liquid distribution pipes 143 is three;
the water mist nozzle 144 is an atomizing nozzle, and the water mist absorption liquid forms atomized absorption liquid with the particle size of about 100-500 mu m in a water mist spraying section through the water mist nozzle 144;
the water spray section 14 is provided with an overflow pipe 17, the upper part of the overflow pipe 17 is provided with a bell mouth, the sectional area of the upper end of the bell mouth is 1.5 times of that of the lower section, and the lower part of the bell mouth is provided with an extension pipe which extends to below the liquid level of the water curtain spray section 12;
the upper part of the water mist spraying section 14 is provided with a secondary dust and mist removing device 15;
communicating pipes are arranged among the water mist absorption liquid distribution pipes 143 and are in flange connection;
the water mist nozzles 144 are annularly arranged in the tower body 1 to realize uniform coverage of the tower section.
As shown in fig. 5, the flue gas treatment system using the deep absorption tower for flue gas treatment in this embodiment includes a main absorption tower 1 and a deep absorption tower 2, the main absorption tower 1 is disposed upstream of the deep absorption tower 2 and is used for chilling flue gas and capturing and reacting particles in the flue gas, a flue gas inlet 11 of the deep absorption tower 2 is connected to an output end of the main absorption tower 1, and a flue gas heater 8 capable of heating the flue gas to a required temperature according to a device configuration is disposed at a flue gas outlet 16 of the deep absorption tower 2.
The main absorption tower 1 is provided with an upper part 21 and a lower part 22 which are communicated with each other, wherein the upper part 21 is used for chilling the flue gas, and the lower part 22 is provided with a large-caliber nozzle to form a foam area which can be in turbulent impact contact with the flue gas and is used for capturing and reacting and absorbing particles in the flue gas.
The flue gas treatment method using the flue gas treatment system in the embodiment comprises the following steps:
the temperature of the flue gas sent from the catalytic cracking battery compartment is 180 ℃, the pressure is about 4KpaG, and the SO in the flue gas2The content is about 3520mg/Nm3(wet basis, same below) dust content of about 230mg/Nm3The flue gas firstly enters the main absorption tower2, a layer of liquid film is formed on the inner wall of the upper part of the main absorption tower 2 by the circulating absorption liquid from the circulating pump 3 of the absorption tower, so that the influence of high-temperature flue gas on the main absorption tower 2 is reduced, and the flue gas is chilled. The flue gas enters the lower part of the main absorption tower 2, the circulating absorption liquid is reversely sprayed out relative to the flue gas through a large-caliber nozzle at the lower part of the main absorption tower 2, a foam area is formed at the lower tower of the main absorption tower 2, the flue gas reversely passes through the foam area and collides with gas-liquid phase micro-clusters in the circulating absorption liquid, and therefore most of SO in the flue gas is enabled to enter2And the particles are enriched in the circulating absorption liquid.
The temperature of the saturated flue gas discharged from the main absorption tower 2 is 58 ℃, and SO in the flue gas2The content is about 168mg/Nm3Dust content of about 40mg/Nm3The flue gas and the circulating absorption liquid enter the deep absorption tower 1 through the connecting section in an inclined way, the flue gas flows along the deep absorption tower from bottom to top, the circulating absorption liquid enters the tower kettle 18 of the deep absorption tower, and soluble salt (in SO) in the circulating absorption liquid4 2-Calculated) the content is 5.5% wt, the concentration of the particulate matter is 1.5g/L, after the particulate matter is pressurized to 0.3-1.0 Mpa (g) by an absorption tower circulating pump 3, the particulate matter is divided into three strands, one strand is sent to the upper part of a main absorption tower 2 to be used as chilling absorption liquid, the other strand is sent to the lower part of the main absorption tower 2 to be used as main circulating absorption liquid, and the third strand is sent out of a boundary area to be used as discharged wastewater, so that the influence of the enrichment of sulfate and the particulate matter in the absorption liquid on the desulfurization and dust removal effects is avoided. The mass flow ratio of the chilling absorption liquid, the main circulation absorption liquid and the discharged wastewater is 1:20: 1;
flue gas enters a water curtain spraying section 12 through a water curtain spraying section air lifting hole 121 arranged in a deep absorption tower 2, a water curtain nozzle 123 is arranged above each air lifting hole 121 of the water curtain spraying section 12, cooled water curtain absorption liquid forms a complete water film above each air lifting hole 121 through the water curtain nozzle 123, the flue gas penetrates out of the water film and is subjected to heat transfer with the water curtain absorption liquid to be cooled to 53 ℃, and SO in the flue gas is further eliminated2The particles and the foam are sent to a first-stage dust and mist eliminator 13, the absorption liquid pumped out from the bottom of the water curtain absorption section 12 and soluble salt (with SO) in the water curtain absorption liquid4 2-Calculated) content of 0.3 percent by weight and particle concentration of 0.15g/L, sending the mixture to a water curtain circulating pump 4 to pressurize to 0.3-1.0 Mpa (g), and absorbing the mixture by a water curtainThe liquid cooler 6 is cooled to 45-55 ℃ and then is sent to the water curtain nozzle 123; the water curtain absorption liquid cooler 6 is a tube type heat exchanger.
The flue gas passes through a first-stage dust and mist eliminator 13 to remove SO in the flue gas after particles above micron level and foam in the flue gas are entrained2The content is about 20mg/Nm3Dust content of about 20mg/Nm3And enters the water mist spraying section 14 through the water mist spraying section air lifting hole. The water mist spraying section 14 is provided with an atomizing nozzle 144, the cooled water mist absorption liquid forms mist drops with the particle size of about 300 mu m in the water mist spraying section 14 through the water mist nozzle 144, when the flue gas passes through the water mist spraying section 14, on one hand, the flue gas is in heat transfer with the water mist absorption liquid and cooled to 47 ℃, on the other hand, submicron-grade particles in the flue gas continuously collide with the atomizing absorption liquid to form large-particle-size micro-clusters which are adsorbed and dissolved in the water mist absorption liquid, and simultaneously, SO in the flue gas is further eliminated2Then the flue gas enters a secondary dust and mist removing device 15, soluble Salt (SO) in the absorption liquid pumped out from the bottom of the water mist spraying section 144 2-Calculated) content of 0.02 wt% and particle concentration of 0.01g/L, sending to a water mist circulating pump 5, pressurizing to 0.3-1.0 Mpa (g), cooling to 40-50 ℃ by a water mist absorption liquid cooler 7, and sending to a water mist nozzle 144. The water mist absorption liquid cooler 7 is a plate heat exchanger or a wound tube heat exchanger.
The flue gas passes through a secondary dust and mist removing device 15 to further remove large-particle-size micro-aggregates formed in the water mist spraying section and water mist carried in the flue gas, and finally SO in the flue gas is discharged2The content is about 10mg/Nm3Dust content of about 5mg/Nm3And is heated by a flue gas heater 8 and then is sent out of a boundary area, and SO in the flue gas2The content is controlled at 5mg/Nm3The content of the particulate matters is controlled within 5mg/Nm3Within.
The flue gas heater 8 is a high-efficiency wound-tube heat exchanger, and hot water at 90 ℃ is used as a heating medium.
And (4) sending the make-up water from the battery limits to a water mist spraying section 14 of the deep absorption tower to be used as system make-up water.
And the alkali liquor from the battery limits is taken as an absorption solvent and is respectively sent to inlet pipelines of an absorption tower circulating pump 3, a water curtain circulating pump 4 and a water mist circulating pump 5. And adjusting the flow of the alkaline solution sent to the inlet of the circulating pump 3 of the absorption tower, and controlling the pH value of the circulating absorption solution to be 5-9. And adjusting the flow of the alkaline solution sent to the inlet of the water curtain circulating pump 4, and controlling the pH value of the water curtain absorption liquid to be 6-10. And adjusting the flow of the alkaline liquor sent to the inlet of the water mist circulating pump 5, and controlling the pH value of the water mist absorption liquid to be 6-10.
In order to avoid the enrichment of particles and sulfate in the water mist absorption liquid, the water mist spraying section 14 is provided with an overflow pipeline 16 which automatically flows to the water curtain spraying section 12; in order to avoid the enrichment of particulate matters and sulfate in the water curtain absorption liquid, the water curtain spraying section 12 is provided with an overflow pipeline 17 which automatically flows to a tower kettle 19 of the deep absorption tower.
Controlling soluble salt (in SO) in the circulating absorption liquid4 2-Calculated) content below 6% wt and a concentration of particulate matter below 3 g/L. And controlling the concentration ratio of the particles in the circulating absorption liquid, the water curtain absorption liquid and the water mist absorption liquid to be 100:10: 1.
Claims (9)
1. The utility model provides a flue gas is handled with degree of depth absorption tower, includes the tower body, its characterized in that: the device comprises a water curtain spraying section, a primary dedusting and demisting section, a water mist spraying section and a secondary dedusting and demisting section which are sequentially arranged from bottom to top, wherein the bottom of a tower body is a liquid collection tower kettle, and the top of the tower body is provided with a flue gas outlet;
the side part of the tower body is provided with a flue gas inlet which is positioned above the tower kettle and below the water curtain spraying section, and the flue gas inlet and the axis of the tower body form an angle of 40-60 degrees;
the bottom of the water curtain spraying section is provided with a first liquid collecting tank capable of separating the water curtain spraying section from a lower area, the water curtain spraying section is provided with a gas lifting hole which vertically extends through the bottom wall of the first liquid collecting tank, and gas below the first liquid collecting tank enters the water curtain spraying section upwards along the gas lifting hole; the top of the water curtain spraying section is provided with water curtain nozzles arranged corresponding to the gas lifting holes;
a second liquid collecting groove capable of separating the water mist spraying section from a water curtain spraying section below the water mist spraying section is formed at the bottom of the water mist spraying section, a gas riser which vertically extends through the bottom wall of the second liquid collecting groove is arranged on the water mist spraying section, gas below the second liquid collecting groove enters the water mist spraying section upwards along the gas riser, the cross section area of the gas riser is larger than that of the gas riser, and an umbrella-shaped cover cap with an upward pointed end is covered above the gas riser; and the water mist spraying section is filled with filler positioned above the gas rising pipe, and a water mist nozzle is arranged above the filler.
2. The deep absorption tower for flue gas treatment according to claim 1, wherein: the gas lift hole be a plurality of and around the tower body center periphery be the shape of returning and arrange, gas lift hole top is provided with horizontal and three cascade absorption liquid distributing pipes that arrange side by side, the rivers nozzle locate on the cascade absorption liquid distributing pipe and with gas lift hole one-to-one, form the cascade that can cover gas lift hole upper end mouth at gas lift hole top.
3. The deep absorption tower for flue gas treatment according to claim 2, wherein: the cascade sprays the section and is provided with the overflow pipe that can lead to the tower cauldron with the hydrops of first catch basin, and this overflow pipe upper portion is provided with the horn mouth, and the upper end cross sectional area of this horn mouth is hypomere cross sectional area 1.5 times, and this overflow pipe lower part extends to main tower cauldron.
4. The deep absorption tower for flue gas treatment according to claim 1, wherein: the air lifting pipes are rectangular, and the six air lifting pipes are arranged in two rows; three transverse water-washing absorption liquid distribution pipes which are arranged side by side are arranged above the gas rising pipe, and the water mist nozzles are arranged on the water-washing absorption liquid distribution pipes.
5. The deep absorption tower for flue gas treatment according to claim 4, wherein: the washing absorption liquid distributing pipe length in the middle is greater than the washing absorption liquid distributing pipe length of both sides, and the washing absorption liquid distributing pipe that is located in the middle is linked together through the liquid pipe and the washing absorption liquid distributing pipe that is located both sides respectively, the water smoke nozzle is a plurality of and connects respectively on the washing absorption liquid distributing pipe, and each washing absorption liquid distributing pipe is arranged jointly and is two annular spray regions that the inside and outside cover was put.
6. A flue gas treatment system using the deep absorption tower for flue gas treatment according to any one of claims 1 to 5, wherein: the deep absorption tower is characterized by comprising a main absorption tower and the deep absorption tower, wherein the main absorption tower is arranged at the upstream of the deep absorption tower and is used for chilling flue gas and capturing and reacting particles in the flue gas to absorb, a flue gas inlet of the deep absorption tower is connected with the output end of the main absorption tower, and a flue gas heater capable of heating the flue gas to the required temperature according to the configuration of the deep absorption tower is arranged at a flue gas outlet of the deep absorption tower.
7. The flue gas treatment system of claim 6, wherein: the main absorption tower is provided with an upper part and a lower part which are communicated with each other, the upper part is used for chilling the flue gas, and the lower part is provided with a large-caliber nozzle to form a foam area which can be in turbulent impact contact with the flue gas and is used for trapping, reacting and absorbing particles in the flue gas.
8. A flue gas treatment process using the flue gas treatment system of claim 6 or 7, characterized by comprising the steps of:
the discharged flue gas sent from the battery compartment firstly enters a main absorption tower, and circulating absorption liquid from an absorption tower circulating pump forms a layer of liquid film on the inner wall of the upper part of the main absorption tower so as to avoid the influence of high-temperature flue gas on the main absorption tower and chill the flue gas; the flue gas then enters the lower part of the main absorption tower, the circulating absorption liquid is reversely sprayed out from the lower part of the main absorption tower through a large-caliber nozzle relative to the flue gas, a foam zone is formed at the lower tower of the main absorption tower, the flue gas reversely passes through the foam zone and collides with gas-liquid phase micro-clusters in the circulating absorption liquid, and therefore most of SO in the flue gas is enabled to be2And the particles are enriched in the circulating absorption liquid; the saturated flue gas and the circulating absorption liquid which are discharged from the main absorption tower obliquely enter the deep absorption tower, the flue gas flows from bottom to top along the deep absorption tower, the circulating absorption liquid enters the tower kettle of the deep absorption tower and is divided into three strands after being pressurized by a circulating pump of the absorption tower, one strand is sent to the upper part of the main absorption tower to be used as chilling absorption liquid, and the other strand is sent to the upper part of the main absorption tower to be used as chilling absorption liquidThe lower part of the main absorption tower is used as main circulation absorption liquid, and the third part of the absorption tower is sent out of a boundary area to be used as discharged wastewater, so that the influence of the enrichment of sulfate and particulate matters in the absorption liquid on the desulfurization and dust removal effects is avoided;
flue gas enters a water curtain spraying section through the arranged water curtain spraying section air lifting holes in the deep absorption tower, a water curtain nozzle is arranged above each air lifting hole in the water curtain spraying section, cooled water curtain absorption liquid forms a complete water film above each air lifting hole through the water curtain nozzle, the flue gas penetrates out of the water film and is subjected to heat transfer with the water curtain absorption liquid to be cooled to 47-57 ℃, and SO in the flue gas is further eliminated2The particles and the entrained foam are sent to a primary dust and mist removing device, and the absorption liquid pumped out from the bottom of the water curtain absorption section is sent to a water curtain circulating pump to be pressurized, then is cooled by a water curtain absorption liquid cooler and then is sent to a water curtain nozzle;
the flue gas passes through a first-stage dust and mist removal device, particles above micron level and foam in the flue gas are removed, and then the flue gas enters a water mist spraying section through a gas lifting hole of the water mist spraying section; the water mist spraying section is provided with an atomizing nozzle, the cooled water mist absorption liquid forms mist drops with the particle size of about 100-500 mu m in the water mist spraying section through the atomizing nozzle, when the flue gas passes through the water mist spraying section, on one hand, the flue gas is subjected to heat transfer and temperature reduction with the water mist absorption liquid, on the other hand, submicron particles in the flue gas continuously collide with the atomizing absorption liquid to form large-particle-size micelles, the large-particle-size micelles are adsorbed and dissolved in the water mist absorption liquid, SO2 in the flue gas is further eliminated, then the flue gas enters a secondary dust removal demister, the absorption liquid extracted from the bottom of the water mist spraying section is sent to a water mist circulating pump to be pressurized, then is sent to the water mist nozzle;
the flue gas passes through a secondary dust and mist removing device to further remove large-particle-size micro-aggregates formed in the water mist spraying section and water mist carried in the flue gas, and the flue gas is heated by a flue gas heater and then sent out of a boundary region, wherein the content of SO2 in the flue gas is controlled at 5mg/Nm3The content of the particulate matters is controlled within 5mg/Nm3Within.
9. The flue gas treatment method according to claim 8, wherein: the mass flow ratio of the chilling absorption liquid to the main circulation absorption liquid to the discharged wastewater is 1 (10-100) to 1.
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Application publication date: 20210115 |