WO2017012557A1 - 一种高效渐变分级复合脱硫塔 - Google Patents

一种高效渐变分级复合脱硫塔 Download PDF

Info

Publication number
WO2017012557A1
WO2017012557A1 PCT/CN2016/090766 CN2016090766W WO2017012557A1 WO 2017012557 A1 WO2017012557 A1 WO 2017012557A1 CN 2016090766 W CN2016090766 W CN 2016090766W WO 2017012557 A1 WO2017012557 A1 WO 2017012557A1
Authority
WO
WIPO (PCT)
Prior art keywords
liquid
desulfurization
slurry
flue gas
layer
Prior art date
Application number
PCT/CN2016/090766
Other languages
English (en)
French (fr)
Inventor
李卫东
赵红
韩长民
何勇
张轶
Original Assignee
华能国际电力股份有限公司
武汉凯迪电力环保有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CN201520530484.0U external-priority patent/CN204841409U/zh
Priority claimed from CN201520778413.2U external-priority patent/CN205007846U/zh
Application filed by 华能国际电力股份有限公司, 武汉凯迪电力环保有限公司 filed Critical 华能国际电力股份有限公司
Priority to US15/577,046 priority Critical patent/US10143957B2/en
Publication of WO2017012557A1 publication Critical patent/WO2017012557A1/zh

Links

Images

Classifications

    • 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
    • B01D47/12—Washers with plural different washing sections
    • 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
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
    • 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
    • B01D47/02—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
    • B01D47/021—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath by bubbling the gas through a liquid bath
    • 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
    • B01D47/06—Spray cleaning
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces

Definitions

  • the invention is based on the inventions of CN201520530484.0 and CN201520778413.2.
  • the invention relates to a desulfurization tower, in particular to an efficient graded graded composite desulfurization tower.
  • the coal-fired flue gas contains a large amount of SO 2 and soot, and also contains a small amount of pollutants such as HCl, HF, SO 3 and heavy metals.
  • the most flue gas desulfurization is the wet flue gas desulfurization device, and the wet flue gas desulfurization Limestone-gypsum wet method is the most widely used.
  • the main function of the limestone-gypsum desulfurization tower is to remove SO 2 and also have the auxiliary function of removing soot and other pollutants.
  • the desulfurization efficiency of wet desulfurization is required to be 90% to 95%.
  • the desulfurization efficiency should exceed 99%, and even higher desulfurization efficiency is required. Therefore, the development of a new desulfurization tower to improve the deep desulfurization performance of the desulfurization tower, so that the SO 2 in the exhaust fumes is lower than 35mg / Nm 3 , and even achieve ultra-low SO 2 emissions below 20mg / Nm 3 , is to solve the medium and high sulfur coal,
  • the important task of high-sulfur coal flue gas treatment has a positive effect on solving the problem of smog and improving air quality.
  • the limestone-gypsum desulfurization tower is generally arranged in the form of a single spray tower in a countercurrent manner.
  • the flue gas enters the absorption tower through the inlet of the absorption tower from the upper part of the slurry tank, passes through the spray layer and the mist eliminator in turn, and is discharged through the chimney.
  • the slurry is sprayed from a plurality of nozzles of each spray layer, moves downward, and undergoes physical and chemical interaction with the flue gas countercurrent contact, and washes and removes sulfur dioxide in the flue gas, and occurs between the dust particles and the liquid droplets in the gas flow. Inertial collision, interception, diffusion, cohesion, and gravity sedimentation cause dust to be trapped.
  • the slurry absorbs sulfur oxides SO 2 , soot and other contaminants from the flue gas and falls into the lower stage of the desulfurization tower, and is forcibly oxidized and crystallized in the slurry tank.
  • the series absorption tower connects the two absorption towers in series through the flue.
  • the flue gas from the boiler induced draft fan first enters the first-stage absorption tower, and some SO 2 in the flue gas is removed by the washing of the first-stage absorption tower, the desulfurization efficiency is generally 30-80%, and the slurry pH is controlled at 4.5-5.3.
  • the main function of this level of absorption is to ensure excellent calcium sulfite oxidation, and sufficient gypsum crystallization time.
  • the oxidizing air coefficient can be greatly reduced, thereby greatly reducing the power consumption of the oxidizing fan, and at the same time greatly improving the quality of the gypsum and increasing the dehydration rate of the gypsum.
  • the flue gas exits the first-stage absorption tower and enters the second-stage absorption tower.
  • the second-stage absorption tower is the main desulfurization washing process. Since the problem of oxidative crystallization is not considered, the pH can be controlled at a very high level, reaching 5.8 ⁇ . 6.4, this makes full use of the performance of the absorbent to remove SO 2 efficiently, and reduces the SO 2 content in the flue gas of the desulfurization tower to a smaller extent.
  • tandem tower technology has achieved the high desulfurization efficiency of medium-high sulfur coal and high-sulfur coal to a certain extent, and solved the problem of reaching the standard discharge, the tandem tower technology also has many shortcomings: 1) the initial investment of the project is high; 2) due to the setting The two-stage absorption tower has a large area. For the transformation of existing equipment, a large number of projects cannot be implemented. 3) There are relatively many equipments, high equipment failure rate, large maintenance and maintenance workload, and high operating cost.
  • the S-type gas-liquid mass transfer mechanism is an upgrade technology based on the S-shaped strip blister-type tray technology in the chemical industry.
  • the conventional S-shaped strip blister plate tray is suitable as a gas-liquid mass transfer device with lower gas velocity, cleaner medium and stable operating conditions. If the technology is directly applied to lime gas gypsum wet desulfurization under higher gas velocity, suspended slurry medium and variable load conditions, there are certain limitations.
  • the flue gas desulfurization technology mostly adopts the empty tower through-flow spray technology, and the following problems exist: on the one hand, the spray slurry directly falls into the bottom of the tower, and can not be collected in stages, and the pH of the slurry has no gradient, when the reaction When the equilibrium point is reached, the desulfurization efficiency is difficult to increase; on the other hand, the fine dust in the flue gas, especially the fine dust of PM2.5 and below, is very low in dust removal efficiency, and the high-speed flue gas will also spray. The fine droplets ejected from the nozzle are carried away, and the gypsum contained in this small droplet also increases the dust emission concentration.
  • the object of the present invention is to provide an efficient grading and grading composite desulfurization tower, which is used for treating medium and high sulfur coal and high sulfur coal flue gas, and has extremely high desulfurization efficiency and dust removal performance.
  • the technical problem to be further solved by the present invention is to provide an efficient graded-graded composite desulfurization tower having an S-shaped strip-shaped blister desulfurization and dust removal tray structure, wherein the S-type gas-liquid mass transfer mechanism has a simple structure and load adaptation. Strong, further improve the dust removal and desulfurization effect, can make desulfurization The effect is further improved to 99.5% or more.
  • the desulfurization efficiency is over 99%, and preferably exceeds 99.5%.
  • the desulfurization tower comprising a tower body, the tower body is provided with a flue gas inlet at a central portion thereof, and a flue gas outlet is opened at the top of the tower body, and the tower body includes oxidation from bottom to top a crystallization section, a crude desulfurization and dust removal section, a fine desulfurization and dust removal section, and a horizontal defogging section;
  • the oxidized crystallization section includes a sump disposed at the bottom of the tower body, and a partitioning mechanism horizontally disposed in the sump and dividing the sump into upper and lower zones, and a plurality of oxidations are disposed in the upper oxidation zone.
  • the coarse desulfurization and dust removal section includes a gas distribution plate disposed above the flue gas inlet, and a multi-layer spray layer disposed above the gas distribution plate, the spray layer being connected to the crystallization zone of the slurry tank;
  • the fine desulfurization and dust removal section includes a tubular mist eliminator, a rinsing layer disposed above the tubular demister, a film holding layer disposed above the rinsing layer, and a liquid holding layer connected to the film holding layer Holding the liquid layer circulation tank, the pH of the slurry in the liquid holding layer circulation tank is greater than the pH value of the slurry in the slurry tank.
  • the film holding layer of the present invention has one of the following three structures:
  • the film holding layer comprises a liquid collector (7), an S-type gas-liquid mass transfer mechanism (8) and a liquid distributor (9), a liquid collector (7) and a liquid holding device arranged in order from bottom to top.
  • the inlet of the layer circulation tank (12) is connected, and the outlet of the liquid-holding layer circulation tank (12) is connected to the liquid distributor (9) through the liquid-holding layer circulation pump (13), or
  • the film holding layer includes an S-type gas-liquid mass transfer mechanism (8) and a liquid distributor (9) disposed in order from bottom to top, and a U-shape in the S-type gas-liquid mass transfer mechanism (8)
  • the collection tank (8031) is connected to the inlet of the liquid-holding layer circulation tank (12), and the outlet of the liquid-holding layer circulation tank (12) is connected to the liquid distributor (9) through the liquid-holding layer circulation pump (13), or
  • the film holding layer includes a liquid collector (7), an S-type gas-liquid mass transfer mechanism (8), and a liquid distributor (9) disposed in order from bottom to top, the liquid collector (7) and
  • the U-shaped collection tank (8031) in the S-type gas-liquid mass transfer mechanism (8) is connected to the inlet of the liquid-holding layer circulation tank (12), the liquid holding The outlet of the layer circulation tank (12) is connected to the liquid distributor (9) via a liquid-holding layer circulation pump (13).
  • the partitioning mechanism is a perforated plate or a plurality of rows of tubes placed side by side.
  • a gas-liquid mass transfer synergy ring is disposed on the inner wall of the tower under each spray layer, and the vertical cross section of the gas-liquid mass transfer effect ring is triangular.
  • the height of the gas-liquid mass transfer effect ring is 300-2000 mm.
  • the nozzle on the spray layer is a single head nozzle or a double head atomizing nozzle.
  • the slurry tank is filled with a gypsum slurry, and the pH of the gypsum slurry is 5.2 to 5.8.
  • the liquid-holding layer circulation tank is filled with a limestone slurry, and the limestone slurry has a pH of 5.8 to 6.4.
  • the S-type gas-liquid mass transfer mechanism comprises at least one U-shaped support member and a tray;
  • the U-shaped support member is fixedly mounted in the absorption tower, the U-shaped support member is provided with a U-shaped collecting groove, and the U-shaped collecting groove is provided with an oxidizing air tube, and the bottom of the oxidizing air tube is opened Vents
  • the tray is vertically installed above the U-shaped support member, and the tray is formed by juxtaposing a plurality of elongated plates having a transverse S-shaped cross section, and the S-shaped end portions of the adjacent plates are mutually arranged. Staggered and spaced apart, the interval constitutes an intermediate passage, the downward opening of the plate body constitutes a flue gas inlet port, the upward opening of the plate body constitutes a flue gas outlet port, and the plate body is located at the flue gas inlet port Gas sealing plates are provided on both sides.
  • the plate body is evenly provided with a tooth gap at the lower edge of the S-shaped end portion in the air outlet of the flue gas.
  • the shape of the tooth gap is rectangular, triangular or trapezoidal.
  • the area of the flue gas outlet is 1.5 to 4 times the area of the intermediate passage.
  • the area of the flue gas inlet is 1 to 4 times the area of the intermediate passage.
  • the bottom gap between the S-shaped end portion of the plate body located in the flue gas outlet and the bottom of the flue gas outlet port exceeds 20 mm.
  • the horizontal defogging section comprises a level 1 to 4 horizontal flue defogger, and the defogger is provided with an independent water rinsing and water recovery unit.
  • the desulfurization tower adopts a grading and grading composite desulfurization technology, has extremely high desulfurization efficiency and dust removal performance, the desulfurization efficiency reaches 99% or more, preferably exceeds 99.5%, and the dust removal efficiency reaches over 90%, which is suitable for the desulfurization tower. It treats medium-high sulfur coal and high-sulfur coal flue gas, especially high-sulfur coal flue gas.
  • the desulfurization tower is a single tower, it is especially suitable for the transformation of existing desulfurization equipment with narrow area and limited land occupation.
  • the limestone slurry having a higher pH value is distributed to the tray through the slurry pipeline connected from the outside of the tower, and the slurry flows to the U in the parallel direction of the plate body.
  • the U-shaped collecting tank flows out of the tower through the slurry pipeline to form a circulation, and the slurry forms a layer of limestone slurry liquid film on the tray;
  • the flue gas enters through the flue gas inlet port because the flue gas inlet port
  • Gas sealing plates are arranged on both sides, so the flue gas can only enter the intermediate passage, and then enter the liquid film layer of the tray through the gap at the bottom of the flue gas outlet, and the flue gas and the slurry are fully mixed to form a foam state or a stable spray state. Reacts with the slurry, increases the mass transfer area, improves the mass transfer effect, and prevents the sedimentation of the slurry particles.
  • the gas and liquid are fully contacted under high pH conditions, which significantly improves the desulfurization efficiency.
  • the oxidizing air can oxidize the sulfite in the U-shaped collecting tank to prevent the formation of sulfate hard scale and sulfite soft scale, on the other hand, the oxidizing air can Stir the slurry to prevent the formation of scale.
  • the invention has the advantages of effective desulfurization function and dust removal function.
  • Figure 1 is a schematic view of the structure of the present invention, wherein Figures 1a - 1c show the arrangement of three liquid-holding layers of the present invention
  • FIG. 2 is a schematic structural view of an S-type gas-liquid mass transfer mechanism in the present invention.
  • Figure 3 is a schematic view showing the structure of a liquid distributor in the present invention.
  • Figure 4 is a schematic view showing the structure of a gas-liquid mass transfer effect ring in the present invention.
  • Figure 5 is a schematic structural view of a gas distribution plate in the present invention.
  • Figure 6 is a schematic view showing the structure of an embodiment of the partitioning mechanism of the present invention.
  • Figure 7 is a schematic structural view of another embodiment of the partitioning mechanism of the present invention.
  • FIGS. 8 to 9 are schematic structural views of a tray in an S-type gas-liquid mass transfer mechanism of the present invention.
  • Figure 10 is a schematic view showing the structure of a gas sealing plate in the S-type gas-liquid mass transfer mechanism of the present invention.
  • Figure 11 is a schematic view of a flue gas passage in an S-type gas-liquid mass transfer mechanism of the present invention.
  • Figure 12a is a schematic view showing the structure of a trapezoidal tooth gap in the S-type gas-liquid mass transfer mechanism of the present invention.
  • Figure 12b is a schematic view showing the structure of a triangular tooth gap in the S-type gas-liquid mass transfer mechanism of the present invention.
  • Figure 12c is a schematic view showing the structure of a rectangular tooth gap in the S-type gas-liquid mass transfer mechanism of the present invention.
  • an efficient grading and grading composite desulfurization tower includes a tower body 17 having a flue gas inlet 1 at the middle of the tower body 17, and a top portion of the tower body 17 The flue gas outlet 11 is opened, and the tower body 17 includes an oxidized crystallization section, a crude desulfurization and dust removal section, a fine desulfurization dust removal section and a horizontal defogging section from bottom to top;
  • the oxidized crystallization section includes a slurry tank disposed at the bottom of the tower body 17, and a partitioning mechanism 16 horizontally disposed in the slurry tank and dividing the slurry tank into upper and lower zones, and a plurality of oxidizing air distribution pipes 15 disposed in the upper oxidation zone. a plurality of agitators 14 disposed in the lower crystallization zone;
  • the coarse desulfurization and dust removal section comprises a gas distribution plate 2 disposed above the flue gas inlet 1 and a multi-layer spray layer 3 disposed above the gas distribution plate 2, and the spray layer 3 is connected to the crystallization zone of the slurry tank;
  • the fine desulfurization and dust removal section comprises a tubular mist eliminator 5, a rinsing layer 6 disposed above the tubular demister 5, a film holding layer disposed above the rinsing layer 6, and a liquid holding layer circulation connected to the film holding layer In the tank 12, the pH of the slurry in the liquid-holding circulation tank 12 is greater than the pH of the slurry in the slurry tank.
  • the film holding layer of the invention has the following structure:
  • the film holding layer comprises a liquid collector (7), an S-type gas-liquid mass transfer mechanism (8) and a liquid distributor (9), a liquid collector (7) and a liquid-holding layer circulation tank, which are disposed in order from bottom to top.
  • the inlet of (12) is connected, and the outlet of the liquid-holding layer circulation tank (12) is connected to the liquid distributor (9) through a liquid-holding layer circulation pump (13).
  • the film holding layer comprises an S-type gas-liquid mass transfer mechanism (8) and a liquid distributor (9) arranged in order from bottom to top, and the S-type gas-liquid mass transfer mechanism (8)
  • the U-shaped collection tank (8031) is connected to the inlet of the liquid-holding layer circulation tank (12), and the outlet of the liquid-holding layer circulation tank (12) is passed through the liquid-holding layer circulation pump (13) and the liquid distributor (9) )connection.
  • the film holding layer comprises a liquid collector (7), an S-type gas-liquid mass transfer mechanism (8) and a liquid distributor (9) disposed in order from bottom to top, the liquid collection
  • the U-shaped collecting tank (8031) in the apparatus (7) and the S-type gas-liquid mass transfer mechanism (8) are both connected to the inlet of the liquid-holding layer circulation tank (12), and the outlet of the liquid-holding layer circulation tank (12) By holding the liquid layer circulation pump (13) and the liquid The cloth (9) is connected.
  • the S-type gas-liquid mass transfer mechanism (8) and/or the liquid collector (7) of the film holding layer of the present invention may each have a slurry collecting function, and therefore, in some embodiments, may be omitted for different purposes.
  • the use of the liquid collector (7) can of course also have both designs, and it is better to perform such a function. It should be further noted that, especially, when the column diameter of the desulfurization tower is small, the liquid collector (7) may be a beneficial redundant design, but when the tower diameter of the desulfurization tower is large, the liquid collector (7) The use is preferred.
  • the partitioning mechanism 16 is a perforated plate 1601 or a plurality of rows of tubes 1602 placed side by side.
  • a gas-liquid mass transfer synergy ring 4 is disposed on the inner wall of the tower body 17 below each spray layer 3, and the gas-liquid mass transfer effect ring 4 is provided.
  • the vertical cross section is a triangle, wherein the height of the gas-liquid mass transfer effect ring 4 is 300 to 2000 mm.
  • the nozzles on the spray layer 3 are single-head nozzles or double-headed atomizing nozzles.
  • the slurry pool is filled with a gypsum slurry having a pH of 5.2 to 5.8.
  • the liquid-holding layer circulation tank 12 is filled with a limestone slurry having a pH of 5.8 to 6.4.
  • an S-type gas-liquid mass transfer mechanism structure the structure includes at least one U-shaped support member 803 and a tray 801;
  • the U-shaped support member 803 is fixedly mounted in the absorption tower 17, and the U-shaped support member 803 is provided with a U-shaped collection groove 8031.
  • the U-shaped collection groove 8031 is provided with an oxidation air tube 811, and the bottom of the oxidation air tube 811 is provided with a plurality of Venting hole
  • the tray 801 is vertically mounted above the U-shaped support member 803.
  • the tray 801 is formed by a plurality of elongated strip-shaped plates 808 having a transverse S-shaped cross section, and the S-shaped end portions 809 of the adjacent plates 808 are formed. Interlaced and spaced apart, the interval constitutes an intermediate passage 806, the downward opening of the plate body 808 constitutes a flue gas inlet 805, the upward opening of the plate body 808 constitutes a flue gas outlet 807, and the plate body 808 is located at the flue gas inlet Gas sealing plates 804 are provided on both sides of the port 805.
  • the lower edge of the S-shaped end portion 809 of the plate body 808 located in the flue gas outlet 807 is uniformly provided with a tooth gap 812.
  • the shape of the serration 812 is rectangular, triangular or trapezoidal.
  • the area of the flue gas outlet 807 is 1.5 to 4 times the area of the intermediate passage 806.
  • the area of the flue gas inlet 805 is 1-4 times the area of the intermediate passage 806. Adjusting the proportion of each channel, adjusting from the traditional close proportional relationship to reduce the area of the intermediate passage, increasing the area of the outlet passage, increasing the flow velocity of the intermediate passage can prevent slurry deposition, and reducing the flow velocity of the outlet passage can prevent the mist entrainment from being large due to excessive injection. .
  • the bottom gap 810 between the S-shaped end 809 and the bottom of the flue gas outlet 807 of the plate body 808 in the flue gas outlet 807 exceeds 20 mm, preferably 20-50 mm. Increase the bottom gap to prevent deposition fouling.
  • the invention is installed on the upper part of the spray tower of the absorption tower, and the U-shaped support member is designed as an U-shaped open upper portion to form a U-shaped collecting tank for collecting the slurry of the tray and taking the function of the slurry collecting tank.
  • the bottom or side of the U-shaped support member is provided with a pipe connection to the slurry pipe, and the collected slurry flows out of the tower through the pipe.
  • the tray is arranged above the U-shaped support member, and is composed of a plurality of adjacent plate bodies covering one piece to form a flue gas inlet port, an intermediate passage and a flue gas outlet port, and the direction of the strip plate body and the U
  • the type of support is vertical.
  • the end of the plate body is provided with a gas sealing plate.
  • the structure of the S-type gas-liquid mass transfer mechanism of the invention can meet the conditions of high gas velocity, suspended slurry medium and variable load of limestone gypsum wet desulfurization, can realize the segmentation collection and segmentation absorption function of the desulfurization tower, and has the structure Simple, stable operation, high efficiency of desulfurization and dust removal, and strong load adaptability.
  • Specific such S-type gas-liquid mass transfer mechanisms have:
  • the higher pH limestone slurry is distributed to the tray through the slurry pipeline connected from the outside of the tray to the tray.
  • the slurry flows along the parallel direction of the plate to the U-shaped collection tank, and then flows out through the pipeline to form a circulation, so that the slurry is in the tray.
  • a layer of limestone slurry liquid film is formed thereon.
  • the direction of liquid flow is changed from the direction of the traditional vertical plate body to the direction of the plate body, and the liquid flow path is smoother to prevent sedimentation of suspended liquid.
  • the flue gas enters the intermediate passage through the flue gas inlet hole, and then enters the tray liquid film layer through the bottom gap level, and leaves the tray disc from the flue gas outlet hole, and the flue gas and the slurry are fully mixed to form a foam state or a stable spray state.
  • the gas velocity range is increased from conventionally lower than 0.8-1.2 m/s to 1 m/s to 3 m/s, and the gas-liquid contact state is changed from the bubble state to the foam state or the stable spray state, which may increase. Large mass transfer area, improve mass transfer effect, while preventing sedimentation of slurry particles.
  • the sufficient contact of gas and liquid under high pH conditions significantly improves the desulfurization efficiency, and the desulfurization efficiency reaches 99.5%. Since the device has the function of collecting the slurry separately, it can realize the partial absorption.
  • the device is arranged on the upper part of the spray layer of the conventional spray desulfurization tower, and the high pH slurry with pH > 5.8 can be used to change the equilibrium condition.
  • the device does not have a large number of fine particle droplets sprayed by the spray tower nozzle by pressure, which reduces the inlet mist drop load of the demister, and also has a good help for improving the defogging effect of the subsequent demister, in the mist.
  • the contribution of suspended gypsum to dust also decreases with decreasing droplet concentration.
  • the load adaptability is strong.
  • the liquid film level, slurry flow rate and slurry pH value of the tray can be adjusted online. These factors are directly related to the desulfurization and dust removal efficiency. Therefore, the desulfurization and dust removal efficiency of the equipment can be adjusted in real time according to the actual load demand.
  • the structure is simple and the operation is stable.
  • the device is a static device and is completed at one time during installation. Through the improvement of the tray, it can effectively adapt to the working conditions of lime gas gypsum wet desulfurization with higher gas velocity, suspended slurry medium and variable load, and the system can run stably for a long time.
  • the horizontal defogging section comprises a level 1 to 4 horizontal flue defogger 10 which is provided with a separate water rinsing and water recovery unit.
  • the bottom slurry tank is divided into an oxidation zone and a crystallization zone by a partition mechanism, and an oxidizing air distribution pipe is disposed in the oxidation zone to ensure efficient oxidation of calcium sulfite in the slurry pool, and an oxidizing air distribution pipe.
  • the alloy material or the non-metal material is used; and the relatively independent crystal region can make the crystal particles of the gypsum grow larger, which not only facilitates the operation of the subsequent dewatering system, but also ensures the defogging effect, improves the desulfurization and dust removal efficiency;
  • a stirrer or other disturbing agitation mechanism can be provided in the zone to prevent gypsum deposits from scaling.
  • the invention adopts the grading and grading composite desulfurization technology, adopts different absorbents in different positions of the desulfurization tower, and the pH value of the slurry also gradually increases from the bottom to the top, especially in the fine desulfurization and dust removal section, the limestone slurry is used as the absorbent, and the pH can be controlled. Very high level, reaching 5.8 ⁇ 6.4, making full use of its high activity, liquid layer circulating tank to provide a higher pH limestone slurry to the film holding layer.
  • the absorbent used in the spray layer is a mixed slurry of limestone-gypsum, and the content of limestone in the mixed liquid gradually increases from the bottom to the top, so the pH of the mixed slurry also gradually increases from the bottom to the top.
  • the flue gas enters the tower through the flue gas inlet, first diffused along the gas distribution plate (the gas distribution plate is a perforated plate) under the obstruction of the gas distribution plate, so that the flow velocity of the tower body is large
  • the flow rate of the small flow rate flue gas is remixed to achieve the effect of flow redistribution, so that the flue gas passing through the gas distribution plate is evenly distributed on the cross section of the tower body, and functions as a uniform flue gas, which can solve the flue gas drift.
  • the problem is to improve the desulfurization and dust removal efficiency; then carry out the crude desulfurization and dust removal under the action of the spray layer, the number of spray layers is 1 to 5 layers, and each layer of the spray layer is provided with an independent circulation pump and a circulation pipeline system, each A gas-liquid mass transfer synergy ring is arranged inside the tower wall below the spray layer, and the nozzle on the spray layer is a single-head nozzle or a double-head atomizing nozzle. If a double-head atomizing nozzle is used, the two outlets are ejected.
  • the spray direction can be the same or vice versa.
  • the fine desulfurization and dust removal section intercepts a large amount of gypsum slurry through a tubular mist eliminator, and then passes through the S-type gas-liquid mass transfer mechanism, which can further improve the mass transfer effect, so that the whole tower has extremely high desulfurization efficiency and dust removal performance, and the total desulfurization tower
  • the desulfurization efficiency can be 99% or more.
  • the SO 2 content at the inlet of the desulfurization tower is 6500 mg/Nm 3
  • the SO 2 content at the outlet of the desulfurization tower can be reduced to 35 mg/Nm 3 or less
  • the SO 2 content at the inlet of the desulfurization tower is 5000 mg/Nm.
  • the SO 2 content at the outlet of the desulfurization tower can be reduced to less than 20 mg/Nm 3 , and the deep desulfurization of the desulfurization tower is realized.
  • the nozzle of the rinse layer faces upward, and the lower portion of the liquid holding layer of the film is washed to prevent the liquid holding layer of the film. The lower part is fouled.
  • the SO 2 and soot gas enters the limestone film slurry layer through the S-type gas-liquid mass transfer mechanism (the limestone slurry liquid film height on the film holding layer is 20-150 mm), which arouses a large number of bubbles to form a foam layer, and SO 2 is
  • the foam layer is absorbed by the slurry, and the smoke is constantly disturbed by the foam while inertia and diffusion, constantly changing direction, increasing the contact probability of the smoke and the liquid, and the smoke is purified.
  • the dust removal effect of the bubbling dust collector has higher dust removal efficiency than the spray tower dust collector, especially the performance of removing fine dust of PM2.5 and below, which is much higher than the dust removal efficiency of the spray layer.
  • the dust removal efficiency of the present invention is increased from 50% to more than 90% of the ordinary desulfurization tower, and the dust content of the desulfurization tower outlet can be reduced to less than 5 mg/Nm 3 , and the desulfurization tower is efficiently dedusted while deep desulfurization is achieved.
  • the desulfurization tower apparatus of the present invention can be industrially used for desulfurization and dust removal.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Treating Waste Gases (AREA)

Abstract

一种高效渐变分级复合脱硫塔，包括塔体（17），塔体（17）内从下至上包括氧化结晶段、粗脱硫除尘段、精脱硫除尘段和水平除雾段；氧化结晶段包括浆池、设置在浆池内并将浆池分为上下两个区的分隔机构（16）；粗脱硫除尘段包括设置在烟气入口（1）上方的气体分布板（2）、多层喷淋层（3），喷淋层（3）与浆池连接；精脱硫除尘段包括管式除雾器（5）、冲洗层（6）、薄膜持液层、持液层循环罐（12），持液层循环罐（12）内浆液的pH值大于浆池内浆液的pH值。

Description

一种高效渐变分级复合脱硫塔
本发明是以CN201520530484.0以及CN201520778413.2两份专利申请为优先权的发明。
技术领域
本发明涉及一种脱硫塔，尤其涉及一种高效渐变分级复合脱硫塔。
背景技术
近几年，我国燃煤电厂为了急于应对国家的环保限值压力，普遍采用价格较高，但是含硫量低、灰份低、热值较高的中低硫煤，适用于中低硫煤(Sar<1.5％)的超低排放技术已成功投产运行。但是，截止目前为止，尚未出现适用于中高、高硫煤(Sar>1.5％)的超低排放技术成功投运的案例。
然而，在我国煤炭资源中有大约30％的煤硫含量在2％以上，尤其西南地区有些煤矿含硫量高达10％，在山西等地区因为经济性、煤质地域性的差异，广泛使用含硫量超过2％的煤质；同时，随着优质煤的使用量日益加剧，我国燃煤电厂将必须面对低硫煤日益减少，燃料成本上升，而被迫使用中高、高硫煤的局面；另外，国家和地方政府加大力度控制火电厂污染物排放浓度，提出了一系列史上严格的排放标准，这些严格的标准也需要具有深度脱硫、高效除尘的高性能脱硫技术来实现。
燃煤烟气中含有大量的SO2、烟尘，还含有少量的HCl、HF、SO3、重金属等污染物，目前烟气脱硫采用最多的是湿法烟气脱硫装置，湿法脱硫中又以石灰石-石膏湿法应用最广。石灰石-石膏法脱硫塔主要功能为脱除SO2，同时也具有脱除烟尘及其它污染物的辅助功能。一般湿法脱硫的脱硫效率要求为90％～95％。在国内，有脱硫效率为98％的成功运行案例，但对于燃用高硫煤机组能达到燃气机组排放要求的湿法脱硫装置，没有使用先例。而国外的湿法脱硫装置，由于其燃煤机组所占的总量不大(与国内相比)，还没有这样高性能的脱硫要求。
对于中高硫煤、高硫煤而言，要实现将脱硫装置出口烟气中SO2含量降低到35mg/Nm3以下，脱硫效率就要超过99％，甚至需要更高的脱硫效率。因此，研发新型脱硫塔，提高脱硫塔的深度脱硫性能，使排放烟气中的SO2低于35mg/Nm3，甚至实现低于20mg/Nm3超低SO2排放，是解决中高硫煤、高硫煤烟气治理的重要任务，对解决雾霾问题，改善大气质量，具有积极的作用。
石灰石-石膏脱硫塔一般采用单个喷淋塔的形式，逆流方式布置。烟气通过吸收塔入口从浆液池上部进入在吸收塔内，依次通过喷淋层、除雾器后，经烟囱排放。浆液由各喷淋层多个喷嘴喷出，向下运动，与烟气逆流接触发生物理及化学作用，对烟气中的二氧化硫进行洗涤脱除，同时气流中的粉尘颗粒与液滴之间发生惯性碰撞、拦截、扩散、凝聚以及重力沉降等作用，使粉尘被捕集。浆液从烟气中吸收硫的氧化物SO2、烟尘以及其它污染物后落入脱硫塔下段浆池，并在浆池中被强制氧化、结晶。
常规石灰石-石膏法脱硫装置的脱硫效率受到限制的主要原因有两个：1)受石膏氧化及结晶、石灰石溶解及控制消耗量等条件的限制，通常吸收浆液的pH值在5.2～5.8之间，限制了吸收剂的活性；2)受单塔的限制，吸收浆液的总流量不能过大，否则将造成塔内液体超负荷，导致烟气压降急剧增大，而无法操作。
为了解决上述问题，串联塔技术受到了一定的应用。串联吸收塔就是把两台吸收塔通过烟道串联起来。锅炉引风机过来的烟气首先进入第一级吸收塔，经过第一级吸收塔的洗涤将烟气中的部分SO2脱除，脱硫效率一般在30～80％，浆液pH控制在4.5～5.3，此级吸收的主要功能是保证优异的亚硫酸钙氧化效果，和充足的石膏结晶时间。特别是对于高硫煤，氧化空气系数可以大大降低，从而大幅降低氧化风机的电耗，并且同时可以大大提高石膏品质，提高石膏脱水率。烟气从第一级吸收塔出来后进入第二级吸收塔，第二级吸收塔是主要的脱硫洗涤过程，由于不用考虑氧化结晶的问题，所以pH可以控制在非常高的水平，达到5.8～6.4，这就充分利用了吸收剂高效脱除SO2的性 能，将脱硫塔出口烟气中SO2的含量降低到更小的范围。
虽然串联塔技术在一定程度上实现了中高硫煤、高硫煤超高的脱硫效率，解决了其达标排放的问题，但串联塔技术也有诸多缺点：1)项目初投资高；2)由于设置两级吸收塔，占地面积大，对于现有装置的改造，大量的项目无法实施；3)设备相对较多，设备故障率高、检修维护工作量大，运行成本高。
此外，S型气液传质机构是在化工领域S形条形泡罩板式塔盘技术基础上的升级技术。常规S形条形泡罩板式塔盘适宜作为较低气速、较干净介质、稳定运行工况条件下的气液传质设备。如果将该技术直接应用于较高气速、悬浮浆液介质、变负荷工况条件下的石灰石石膏湿法脱硫，则存在一定的局限性。
然而，目前烟气脱硫技术多采用空塔穿流喷淋技术，存在以下问题：一方面喷淋浆液直接落入塔底浆池，不能分段收集分段吸收，浆液pH值没有梯度，当反应趋向平衡点时脱硫效率难以再提高；另一方面，喷淋洗涤对烟气中的细小粉尘，特别是PM2.5及以下细小粉尘，除尘效率很低，而且，高速烟气还会将喷淋喷嘴喷出的细小液滴带走，这部分细小液滴所含的石膏也增加了粉尘排放浓度。
基于以上本领域中脱硫塔所存在的问题，因此，提出了以下本发明的技术内容。
发明内容
发明要解决的问题
本发明的目的在于提供一种高效渐变分级复合脱硫塔，它用于处理中高硫煤、高硫煤烟气，具有极高的脱硫效率及除尘性能。
此外，本发明还进一步要解决的技术问题在于，提供具有一种S形条形泡罩脱硫除尘塔盘结构的高效渐变分级复合脱硫塔，所述S型气液传质机构结构简单，负荷适应性强，进一步的提高了除尘和脱硫效果，可以使得脱硫 效果进一步的提高到99.5％以上。
因此，通过本发明的脱硫塔，脱硫效率超99％，且优选超过99.5％
用于解决问题的方案
本发明解决其技术问题所采用的技术方案是：
提供一种高效渐变分级复合脱硫塔，该脱硫塔包括塔体，所述塔体的中部开设有烟气入口，所述塔体的顶部开设有烟气出口，所述塔体内从下至上包括氧化结晶段、粗脱硫除尘段、精脱硫除尘段和水平除雾段；其中，
所述氧化结晶段包括设置在塔体底部的浆池、以及水平设置在所述浆池内并将所述浆池分为上下两个区的分隔机构，位于上部的氧化区内设置有多根氧化空气分布管，位于下部的结晶区内设置有多个搅拌器；
所述粗脱硫除尘段包括设置在烟气入口上方的气体分布板、设置在所述气体分布板上方的多层喷淋层，所述喷淋层与浆池结晶区连接；
所述精脱硫除尘段包括管式除雾器、设置在所述管式除雾器上方的冲洗层、设置在所述冲洗层上方的薄膜持液层、以及与所述薄膜持液层连接的持液层循环罐，所述持液层循环罐内浆液的pH值大于浆池内浆液的pH值。
本发明的薄膜持液层具有如下三种结构之一：
(a)所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气液传质机构(8)和液体分布器(9)，液体收集器(7)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接，或者，
(b)所述薄膜持液层包括从下至上依次设置的S型气液传质机构(8)和液体分布器(9)，所述S型气液传质机构(8)中的U型收集槽(8031)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接，或者，
(c)所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气液传质机构(8)和液体分布器(9)，所述液体收集器(7)以及S型气液传质机构(8)中的U型收集槽(8031)均与持液层循环罐(12)的入口连接，所述持液 层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接。
按上述技术方案，所述分隔机构为多孔板、或并排放置的多根排管。
按上述技术方案，所述塔体内壁上位于每层喷淋层的下方设置气液传质增效环，所述气液传质增效环的竖直截面为三角形。
按上述技术方案，所述气液传质增效环的高度为300～2000mm。
按上述技术方案，所述喷淋层上的喷嘴为单头喷嘴或双头雾化喷嘴。
按上述技术方案，所述浆池内装有石膏浆液，所述石膏浆液的pH值为5.2～5.8。
按上述技术方案，所述持液层循环罐内装有石灰石浆液，所述石灰石浆液的PH值为5.8～6.4。
按上述技术方案，所述S型气液传质机构包括至少一个U型支撑件和塔盘；
所述U型支撑件固定安装在吸收塔内，所述U型支撑件上设有U型收集槽，所述U型收集槽内安装有氧化空气管，所述氧化空气管的底部开设有多个出气孔；
所述塔盘垂直安装在所述U型支撑件的上方，所述塔盘由多个截面为横向S形的长条形板体并列排布而成，相邻板体间S型端部相互交错并间隔设置，该间隔构成中间通道，所述板体向下的开口构成烟气进气口，所述板体向上的开口构成烟气出气口，所述板体上位于烟气进气口的两侧设有气体密封板。
按上述技术方案，所述板体位于烟气出气口内的S型端部下缘均匀开设有齿缝。
按上述技术方案，所述齿缝的形状为矩形、三角形或梯形。
按上述技术方案，所述烟气出气口的面积是中间通道的面积的1.5～4倍。
按上述技术方案，所述烟气进气口的面积是中间通道的面积的1～4倍。
按上述技术方案，所述板体位于烟气出气口内的S型端部与烟气出气口底部之间的底部间隙超过20mm。
按上述技术方案，所述水平除雾段包括1～4级水平烟道除雾器，该除雾器设有独立的水冲洗及水回收单元。
发明的效果
本发明，具有以下有益效果：该脱硫塔采用渐变分级复合脱硫技术，具有极高的脱硫效率和除尘性能，脱硫效率达到99％以上，优选超过99.5％，除尘效率达到90％以上，适合用于处理中高硫煤、高硫煤烟气，尤其是处理高硫煤烟气，同时，由于该脱硫塔是单塔，特别适合于区域狭窄、占地受限的现有脱硫装置改造。
特别的，本发明中的独特的S型气液传质机构在工作时，较高pH值的石灰石浆液通过上方接自塔外的浆液管道分布到塔盘，浆液沿板体平行方向流至U型收集槽内，U型收集槽再通过浆液管道流出塔外形成循环，同时浆液在塔盘上形成一层石灰石浆液液膜；烟气经烟气进气口进入，因为烟气进气口的两侧设有气体密封板，因此烟气只能进入中间通道，再通过烟气出气口底部间隙水平进入塔盘液膜层，烟气与浆液充分混合，形成泡沫态或者是稳定的喷射态并与浆液发生反应，增大传质面积，提高传质效果，同时防止浆液颗粒沉积，气液在高pH值条件下充分接触，显著提高脱硫效率。
同时，通过在U型收集槽内设置氧化空气管，一方面氧化空气可以氧化U型收集槽内的亚硫酸盐，防止硫酸盐硬垢和亚硫酸盐软垢的生成，另一方面氧化空气可以对浆液进行搅拌，防止沉积垢的生成。本发明具有脱硫功能和除尘功能得到有效的增强。
附图说明
下面将结合附图及实施例对本发明作进一步说明，附图中：
图1是本发明的结构示意图，其中图1a-图1c表示了本发明三种薄膜持液层的设置；
图2是本发明中S型气液传质机构的结构示意图；
图3是本发明中液体分布器的结构示意图；
图4是本发明中气液传质增效环的结构示意图；
图5是本发明中气体分布板的结构示意图；
图6是本发明中分隔机构一个实施例的结构示意图；
图7是本发明中分隔机构另一个实施例的结构示意图；
图8-图9是本发明中S型气液传质机构中塔盘的结构示意图；
图10是本发明中S型气液传质机构中气体密封板的结构示意图；
图11是本发明中S型气液传质机构中烟气通道的示意图；
图12a是本发明中S型气液传质机构中梯形齿缝的结构示意图；
图12b是本发明中S型气液传质机构中三角形齿缝的结构示意图；
图12c是本发明中S型气液传质机构中矩形齿缝的结构示意图。
附图标记说明
图中：1-烟气入口、2-气体分布板、3-喷淋层、4-气液传质增效环、5-管式除雾器、6-冲洗层、7-液体收集器、8-S型气液传质机构、9-液体分布器、10-水平烟道除雾器、11-烟气出口、12-持液层循环罐、13-持液层循环泵、14-搅拌器、15-氧化空气分布管、16-分隔机构、1601-多孔板、1602-排管、17-塔体。
801-塔盘、803-U型支撑件、8031-U型收集槽、804-气体密封板、805-烟气进气口、806-中间通道、807-烟气出气口、808-板体、809-S型端部、810-底部间隙、811-氧化空气管、812-齿缝。
具体实施方式
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图及实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅用以解释本发明，并不用于限定本发明。
在本发明的较佳实施例中，如图1a所示，一种高效渐变分级复合脱硫塔，该脱硫塔包括塔体17，塔体17的中部开设有烟气入口1，塔体17的顶部开设有烟气出口11，塔体17内从下至上包括氧化结晶段、粗脱硫除尘段、精脱硫除尘段和水平除雾段；其中，
氧化结晶段包括设置在塔体17底部的浆池、以及水平设置在浆池内并将浆池分为上下两个区的分隔机构16，位于上部的氧化区内设置有多根氧化空气分布管15，位于下部的结晶区内设置有多个搅拌器14；
粗脱硫除尘段包括设置在烟气入口1上方的气体分布板2、设置在气体分布板2上方的多层喷淋层3，喷淋层3与浆池结晶区连接；
精脱硫除尘段包括管式除雾器5、设置在管式除雾器5上方的冲洗层6、设置在冲洗层6上方的薄膜持液层、以及与薄膜持液层连接的持液层循环罐12，持液层循环罐12内浆液的pH值大于浆池内浆液的pH值。
本发明的一种实施方式中，本发明的薄膜持液层具有如下结构：
所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气液传质机构(8)和液体分布器(9)，液体收集器(7)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接。
在另外一种实施方式中，所述薄膜持液层包括从下至上依次设置的S型气液传质机构(8)和液体分布器(9)，所述S型气液传质机构(8)中的U型收集槽(8031)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接。
在另外一种实施方式中，所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气液传质机构(8)和液体分布器(9)，所述液体收集器(7)以及S型气液传质机构(8)中的U型收集槽(8031)均与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分 布器(9)连接。
本发明中薄膜持液层的S型气液传质机构(8)和/或液体收集器(7)均可以具有浆液收集功能，因此，在一些实施方式中，出于不同的目的，可以省略液体收集器(7)的使用，当然也可以同时兼有两者的设计，更好的起到这样的功能。需要进一步说明的是，尤其的，当脱硫塔的塔直径较小时，液体收集器(7)可能是一种有益的冗余设计，但脱硫塔的塔直径较大时，液体收集器(7)的使用是优选的。
在本发明的优选实施例中，如图6、图7所示，分隔机构16为多孔板1601、或并排放置的多根排管1602。
在本发明的优选实施例中，如图1a、图4所示，塔体17内壁上位于每层喷淋层3的下方设置气液传质增效环4，气液传质增效环4的竖直截面为三角形，其中，气液传质增效环4的高度为300～2000mm。
在本发明的优选实施例中，如图1a所示，喷淋层3上的喷嘴为单头喷嘴或双头雾化喷嘴。
在本发明的优选实施例中，如图1a所示，浆池内装有石膏浆液，石膏浆液的pH值为5.2～5.8。
在本发明的优选实施例中，如图1a所示，持液层循环罐12内装有石灰石浆液，石灰石浆液的pH值为5.8～6.4。
在本发明的较佳实施例中，如图2、图8-图12所示，一种S型气液传质机构结构，该结构包括至少一个U型支撑件803和塔盘801；
U型支撑件803固定安装在吸收塔17内，U型支撑件803上设有U型收集槽8031，U型收集槽8031内安装有氧化空气管811，氧化空气管811的底部开设有多个出气孔；
塔盘801垂直安装在U型支撑件803的上方，塔盘801由多个截面为横向S形的长条形板体808并列排布而成，相邻板体808间S型端部809相 互交错并间隔设置，该间隔构成中间通道806，板体808向下的开口构成烟气进气口805，板体808向上的开口构成烟气出气口807，板体808上位于烟气进气口805的两侧设有气体密封板804。
本发明的优选实施例中，如图12a-图12c所示，板体808位于烟气出气口807内的S型端部809下缘均匀开设有齿缝812。
本发明的优选实施例中，如图12a-图12c所示，齿缝812的形状为矩形、三角形或梯形。
本发明的优选实施例中，如图11所示，烟气出气口807的面积是中间通道806的面积的1.5～4倍。烟气进气口805的面积是中间通道806的面积的1～4倍。调整各通道比例，由传统的接近等比例关系调整为减少中间通道面积，增大出口通道面积，中间通道流速提高可以防止浆液沉积，出口通道流速降低可以防止因喷射过高导致雾沫夹带量大。
本发明的优选实施例中，如图11所示，板体808位于烟气出气口807内的S型端部809与烟气出气口807底部之间的底部间隙810超过20mm，优选20-50mm，增加该底部间隙，可以防止沉积结垢堵塞。
本发明安装在吸收塔喷淋层的上部，U型支撑件设计成上部敞口的U形，形成U型收集槽，用于收集塔盘浆液，承担浆液收集槽的功能。U型支撑件的底部或侧部设有管道接口与浆液管道连接，收集的浆液通过管道流出塔外。塔盘设置在U型支撑件上方，由多个相邻的板体一件覆盖一件地组成，形成烟气进气口、中间通道和烟气出气口，且条形板体的方向与U型支撑件垂直。板体的端部设有气体密封板。
本发明的S型气液传质机构结构能满足石灰石石膏湿法脱硫较高气速、悬浮浆液介质、变负荷的工况条件，能实现脱硫塔的分段收集和分段吸收功能，具有结构简单，运行稳定，脱硫除尘效率高，负荷适应性强的特点。具体的这样的S型气液传质机构具有：
(1)高效脱硫功能。较高pH值的石灰石浆液通过塔盘上方接自塔外的浆液管道分布到塔盘，浆液沿板体平行方向流至U型收集槽，再通过管道流出塔外形成循环，这样浆液在塔盘上形成一层石灰石浆液液膜。液体流动方向由传统垂直板体方向改为与板体方向一致，液体流道更畅通，防止悬浮液体沉积结垢。烟气通过烟气进气孔进入中间通道，再通过底部间隙水平进入塔盘液膜层，从烟气出气孔离开塔盘，烟气与浆液充分混合，形成泡沫态或者是稳定的喷射态并与浆液发生反应，气速范围由常规低于0.8～1.2m/s提高为1m/s～3m/s之间，气液接触状态由鼓泡态转为泡沫态或稳定的喷射态，可以增大传质面积，提高传质效果，同时防止浆液颗粒沉积。气液在高pH值条件下的充分接触，显著提高脱硫效率，脱硫效率达99.5％。因该装置具有收集浆液单独循环的功能，因此可以实现分段吸收，该装置布置在常规喷淋脱硫塔喷淋层上部，可以采用pH＞5.8的高pH值浆液，改变平衡条件。
(2)高效除尘功能。塔盘上部形成了全覆盖的液膜，当气体通过齿缝水平进入液膜时，激起大量气泡，增加了气液接触面积，而且粉尘在惯性、扩散作用的同时又不断地受到泡沫的扰动，使粉尘不断改变方向，增加了粉尘与液体的接触机会，粉尘得到进一步脱除。由于该装置的除尘包括气泡、液膜对粉尘的捕集作用，其除尘效果比喷淋的除尘效率高，尤其是脱除PM2.5及以下细小粉尘的性能很高，远高于喷淋洗涤的除尘效率。同时，该装置没有喷淋塔喷嘴利用压力喷射出的大量细颗粒雾滴作用，减少了除雾器的入口雾滴负荷，对提高后续除雾器的除雾效果也有良好的帮助，雾滴中悬浮石膏对粉尘的贡献也随雾滴浓度的降低而减少。
(3)负荷适应性强。塔盘的液膜液位、浆液流量及浆液pH值均可以实现在线调节，这几个因素与脱硫除尘效率直接相关，因此该设备的脱硫除尘效率可以根据实际负荷需求实时调节。
(4)结构简单、运行稳定。该装置属静设备，在安装期间一次完成。 通过对塔盘的改进，能有效适应石灰石石膏湿法脱硫较高气速、悬浮浆液介质、变负荷的工况条件，系统可长期稳定运行。
另外，在本发明的优选实施例中，如图1a所示，水平除雾段包括1～4级水平烟道除雾器10，该除雾器设有独立的水冲洗及水回收单元。
此外，本发明在使用时，底部的浆池通过分隔机构分为氧化区和结晶区，并在氧化区内设置氧化空气分布管，以保证浆池中亚硫酸钙的高效氧化，氧化空气分布管采用合金材料或非金属材料；而相对独立的结晶区可以使石膏的结晶颗粒长得更大，不仅有利于后续脱水系统的操作，还能保证除雾效果，提高脱硫和除尘效率；另，结晶区内可以设置搅拌器或其他扰动式搅拌机构，用于防止石膏沉积结垢。
本发明采用渐变分级复合脱硫技术，在脱硫塔不同的位置采用不同的吸收剂，浆液的pH值也由下向上逐渐增加，尤其是在精脱硫除尘段采用石灰石浆液作为吸收剂，pH可以控制在非常高的水平，达到5.8～6.4，充分利用了其高活性，持液层循环罐向薄膜持液层提供pH值较高的石灰石浆液。喷淋层使用的吸收剂为石灰石-石膏的混合浆液，而石灰石在混合液中的含量由下向上逐渐增加，因此混合浆液的pH值也由下向上逐渐增加。
工作时，烟气经烟气入口进入塔内，先在气体分布板的阻碍下，沿着气体分布板(气体分布板为多孔板)向四周扩散，使得塔体截面上较大流速烟气和较小流速烟气的流速进行再混合，达到流量再分配的作用，使通过气体分布板后的烟气在塔体截面上分配均匀，起到均布烟气的作用，可以解决烟气偏流的问题，提高脱硫和除尘效率；然后在喷淋层的作用下进行粗脱硫除尘，喷淋层的数量为1～5层，每层喷淋层设有独立的循环泵及循环管路系统，每个喷淋层下方的塔壁内侧设有气液传质增效环，喷淋层上的喷嘴为单头喷嘴或双头雾化喷嘴，若采用双头雾化喷嘴，其两个出口喷出来的喷雾方向可以相同，也可以相反。
精脱硫除尘段通过管式除雾器拦截大量的石膏浆液，再通过S型气液传质机构，可以进一步提高传质效果，使整塔具有极高的脱硫效率和除尘性能，脱硫塔的总脱硫效率可以实现99％或99.5％以上，在脱硫塔入口SO2含量为6500mg/Nm3，脱硫塔出口SO2含量可以降低到35mg/Nm3以下，在脱硫塔入口SO2含量为5000mg/Nm3时，脱硫塔出口SO2含量可以降低到20mg/Nm3以下，实现了脱硫塔的深度脱硫，另，冲洗层的喷嘴朝上，对薄膜持液层的下部冲洗，以防止薄膜持液层下部结垢。同时，含SO2和烟尘气体通过S型气液传质机构进入石灰石薄膜浆液层(薄膜持液层上石灰石浆液液膜高度为20～150mm)，激起大量的气泡形成泡沫层，SO2在泡沫层被浆液吸收，而烟尘在惯性、扩散作用的同时又不断地受到泡沫的扰动，不断改变方向，增加了烟尘与液体的接触机率，烟气得到净化。鼓泡式除尘器的除尘效果比喷雾塔除尘器具有更高的除尘效率，尤其是脱除PM2.5及以下细小烟尘的性能很高，远高于喷淋层的除尘效率。因此，本发明的除尘效率从普通脱硫塔的50％提高到90％以上，脱硫塔出口烟尘含量可以降低到5mg/Nm3以下，在深度脱硫的同时实现了脱硫塔的高效除尘。
应当理解的是，对本领域普通技术人员来说，可以根据上述说明加以改进或变换，而所有这些改进和变换都应属于本发明所附权利要求的保护范围。
产业上的可利用性
本发明的脱硫塔装置可以在工业上进行脱硫除尘而被实际应用。

Claims (14)

  1. 一种高效渐变分级复合脱硫塔，该脱硫塔包括塔体(17)，所述塔体(17)的中部开设有烟气入口(1)，所述塔体(17)的顶部开设有烟气出口(11)，其特征在于，所述塔体(17)内从下至上包括氧化结晶段、粗脱硫除尘段、精脱硫除尘段和水平除雾段；其中，
    所述氧化结晶段包括设置在塔体(17)底部的浆池、以及水平设置在所述浆池内并将所述浆池分为上下两个区的分隔机构(16)，位于上部的氧化区内设置有多根氧化空气分布管(15)，位于下部的结晶区内设置有多个搅拌器(14)；
    所述粗脱硫除尘段包括设置在烟气入口(1)上方的气体分布板(2)、设置在所述气体分布板(2)上方的多层喷淋层(3)，所述喷淋层(3)与浆池结晶区连接；
    所述精脱硫除尘段包括管式除雾器(5)、设置在所述管式除雾器(5)上方的冲洗层(6)、设置在所述冲洗层(6)上方的薄膜持液层、以及与所述薄膜持液层连接的持液层循环罐(12)，所述持液层循环罐(12)内浆液的pH值大于浆池内浆液的pH值，
    所述薄膜持液层具有如下三种结构之一：
    (a)所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气液传质机构(8)和液体分布器(9)，液体收集器(7)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接；或者，
    (b)所述薄膜持液层包括从下至上依次设置的S型气液传质机构(8)和液体分布器(9)，所述S型气液传质机构(8)中的U型收集槽(8031)与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接；或者，
    (c)所述薄膜持液层包括从下至上依次设置的液体收集器(7)、S型气 液传质机构(8)和液体分布器(9)，所述液体收集器(7)以及S型气液传质机构(8)中的U型收集槽(8031)均与持液层循环罐(12)的入口连接，所述持液层循环罐(12)的出口通过持液层循环泵(13)与液体分布器(9)连接。
  2. 根据权利要求1所述的脱硫塔，其特征在于，所述分隔机构(16)为多孔板、或并排放置的多根排管。
  3. 根据权利要求1或2所述的脱硫塔，其特征在于，所述塔体(17)内壁上位于每层喷淋层(3)的下方设置气液传质增效环(4)，所述气液传质增效环(4)的竖直截面为三角形。
  4. 根据权利要求3所述的脱硫塔，其特征在于，所述气液传质增效环(4)的高度为300～2000mm。
  5. 根据权利要求1-4任一项所述的脱硫塔，其特征在于，所述喷淋层(3)上的喷嘴为单头喷嘴或双头雾化喷嘴。
  6. 根据权利要求1-5任一项所述的脱硫塔，其特征在于，所述浆池内装有石膏浆液，所述石膏浆液的pH值为5.2～5.8。
  7. 根据权利要求1-6任一项所述的脱硫塔，其特征在于，所述持液层循环罐(12)内装有石灰石浆液，所述石灰石浆液的pH值为5.8～6.4。
  8. 根据权利要求1-7任一项所述的脱硫塔，其特征在于，所述S型气液传质机构(8)包括至少一个U型支撑件(803)和塔盘(801)；
    所述U型支撑件(803)固定安装在吸收塔内，所述U型支撑件(803)上设有U型收集槽(8031)，所述U型收集槽(8031)内安装有氧化空气管(811)，所述氧化空气管(811)的底部开设有多个出气孔；
    所述塔盘(801)垂直安装在所述U型支撑件(803)的上方，所述塔盘(801)由多个截面为横向S形的长条形板体(808)并列排布而成，相邻板体间S型端部相互交错并间隔设置，该间隔构成中间通道(806)，所述板体(808)向下的开口构成烟气进气口(805)，所述板体(808)向上的开口构 成烟气出气口(807)，所述板体(808)上位于烟气进气口(805)的两侧设有气体密封板(804)。
  9. 根据权利要求8所述的脱硫塔，其特征在于，所述板体(808)位于烟气出气口(807)内的S型端部下缘均匀开设有齿缝。
  10. 根据权利要求9所述的脱硫塔，其特征在于，所述齿缝的形状为矩形、三角形或梯形。
  11. 根据权利要求8-10任一项所述的脱硫塔，其特征在于，所述烟气出气口(807)的面积是中间通道(806)的面积的1.5～4倍。
  12. 根据权利要求8-11任一项所述的脱硫塔，其特征在于，所述烟气进气口(805)的面积是中间通道(806)的面积的1～4倍。
  13. 根据权利要求18-12任一项所述的脱硫塔，其特征在于，所述板体(808)位于烟气出气口(807)内的S型端部与烟气出气口(807)底部之间的底部间(810)隙超过20mm。
  14. 根据权利要求1-13任一项所述的脱硫塔，其特征在于，所述水平除雾段包括1～4级水平烟道除雾器(10)，该除雾器设有独立的水冲洗及水回收单元。
PCT/CN2016/090766 2015-07-21 2016-07-20 一种高效渐变分级复合脱硫塔 WO2017012557A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US15/577,046 US10143957B2 (en) 2015-07-21 2016-07-20 High-efficiency gradient hierarchy complex desulfurizing tower

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN201520530484.0U CN204841409U (zh) 2015-07-21 2015-07-21 高效渐变分级复合脱硫塔
CN201520530484.0 2015-07-21
CN201520778413.2 2015-10-09
CN201520778413.2U CN205007846U (zh) 2015-10-09 2015-10-09 S形条形泡罩脱硫除尘塔盘结构

Publications (1)

Publication Number Publication Date
WO2017012557A1 true WO2017012557A1 (zh) 2017-01-26

Family

ID=57834984

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2016/090766 WO2017012557A1 (zh) 2015-07-21 2016-07-20 一种高效渐变分级复合脱硫塔

Country Status (2)

Country Link
US (1) US10143957B2 (zh)
WO (1) WO2017012557A1 (zh)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106621722A (zh) * 2017-02-16 2017-05-10 山东神华山大能源环境有限公司 一种用于湿法脱硫塔内的浆液隔离装置及脱硫塔
CN106902629A (zh) * 2017-05-03 2017-06-30 无锡翱翔环保机械有限公司 脱硫塔环形布水装置
CN108211749A (zh) * 2018-03-28 2018-06-29 李文 一种湿法脱硫喷淋塔及脱硫方法
CN109173667A (zh) * 2018-09-25 2019-01-11 内蒙古弘睿节能科技有限公司 一种全自动三级脱硫除尘装置
CN109200718A (zh) * 2018-09-28 2019-01-15 北京国电龙源环保工程有限公司 湿法脱硫除尘系统及其自动冲洗、布水和补水控制方法
CN109432974A (zh) * 2018-12-25 2019-03-08 武汉森源蓝天环境科技工程有限公司 一种鼓泡式自动循环湿法烟气脱硫装置
CN109453641A (zh) * 2018-12-29 2019-03-12 西安科技大学 煤矿井下超声波雾化除硫装置
CN109806754A (zh) * 2017-11-21 2019-05-28 国电环境保护研究院有限公司 一种脱硫吸收塔装置
CN110433594A (zh) * 2019-09-12 2019-11-12 佛山市顺德区东波环保设备有限公司 一种脱硫脱硝环保烟气处理用反应塔
CN110530162A (zh) * 2018-07-13 2019-12-03 韶关市力高机械制造有限公司 应用于冲天炉的除尘系统
CN116059752A (zh) * 2023-02-03 2023-05-05 江苏申正建设工程有限公司 一种烟气除尘脱硫塔及除尘脱硫工艺

Families Citing this family (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3706882A4 (en) * 2017-11-08 2021-08-18 BTU International, Inc. DEVICES, SYSTEMS AND METHODS FOR REMOVING FLUX FROM A FURNACE PROCESS GAS
CN108786423B (zh) * 2018-08-10 2024-05-28 西安航天源动力工程有限公司 一种烟气综合治理方法及装置
CN108970383A (zh) * 2018-09-19 2018-12-11 合肥水泥研究设计院有限公司 一种具有双级气流分布装置的烟气脱硫吸收塔
CN109433150B (zh) * 2018-12-20 2024-04-26 中冶焦耐(大连)工程技术有限公司 一种自支撑组合塔盘
CN109316890A (zh) * 2018-12-26 2019-02-12 北京国电龙源环保工程有限公司 一种脱硫超低排放改造的高效耦合除尘除雾装置
CN109663490A (zh) * 2018-12-30 2019-04-23 福建龙净环保股份有限公司 具有水平衡功能的湿法脱硫烟气冷凝系统及烟气冷凝方法
CN109529596A (zh) * 2019-01-22 2019-03-29 中建材环保研究院（江苏）有限公司 一种改良的sda半干法脱硫塔
CN109925854B (zh) * 2019-03-21 2022-12-02 扬州石化有限责任公司 一种用于石油催化裂化过程中的脱硫装置
CN110052157A (zh) * 2019-04-01 2019-07-26 浙江菲达环保科技股份有限公司 一种基于改性赤泥的Hg、SO3协同脱除装置
CN110508039A (zh) * 2019-08-23 2019-11-29 上海中芬新能源投资有限公司 一种具有初级除雾功能的吸收塔除雾器冲洗水收集装置
CN110479077B (zh) * 2019-09-17 2024-05-03 上海蓝科石化环保科技股份有限公司 一种氨法脱硫氧化装置及方法
CN110665361A (zh) * 2019-10-30 2020-01-10 哈尔滨蔚蓝环保设备制造有限公司 一种除尘脱硫一体化的超低排放设备
CN111408257A (zh) * 2020-04-14 2020-07-14 大唐环境产业集团股份有限公司 一种新型管道支撑结构
CN111715046A (zh) * 2020-07-20 2020-09-29 清远市嘉禾稀有金属有限公司 一种抽吸式溶矿酸雾喷淋塔
CN111841252A (zh) * 2020-07-22 2020-10-30 余东伟 一种基于化工降膜吸收塔用的气液分布系统装置
CN112426841B (zh) * 2020-11-11 2022-11-18 昆岳互联环境技术(江苏)有限公司 数字化脱硫除雾器冲洗控制装置及方法
CN112588093A (zh) * 2020-11-24 2021-04-02 安徽格绿恩环保工程科技有限公司 一种双碱法脱硫工艺
CN112604489A (zh) * 2020-12-07 2021-04-06 昆岳互联环境技术(江苏)有限公司 一种可根据变化量调整运行参数的湿法烟气脱硫装置
CN114669180A (zh) * 2022-03-02 2022-06-28 南京大学环境规划设计研究院集团股份公司 一种吸收VOCs的装置
CN114950118A (zh) * 2022-05-18 2022-08-30 华电电力科学研究院有限公司 一种湿法脱硫用的喷淋系统
CN114911169A (zh) * 2022-06-13 2022-08-16 大唐环境产业集团股份有限公司 一种脱硫增效装置的优化方法、系统、设备及介质
CN116099348A (zh) * 2023-02-15 2023-05-12 武汉科技大学 一种提高脱硫效率的多层喷淋脱硫塔
CN117547917B (zh) * 2024-01-09 2024-03-19 云南凯瑞特工程机械设备有限公司 用于筛分站的水雾除尘设备

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2546068Y (zh) * 2001-03-29 2003-04-23 许开天 喷射态顺流组合型板式化工塔器
CN2568291Y (zh) * 2002-09-09 2003-08-27 华东理工大学 多功能脱硫塔
CN2705221Y (zh) * 2004-05-21 2005-06-22 四川乐山禹伽茶业科技开发有限公司 一种自吸式条形泡罩蒸馏塔
CN201669053U (zh) * 2010-05-17 2010-12-15 上海申川环保科技有限公司 设有烟气水洗构件的脱硫装置
CN103623682A (zh) * 2013-12-16 2014-03-12 张继惟 一种用于烟气净化的hc-lscr／o-as工程系统
CN104107628A (zh) * 2014-07-10 2014-10-22 中国神华能源股份有限公司 一种烟气脱硫设备及其方法
CN204469533U (zh) * 2015-01-28 2015-07-15 华能国际电力股份有限公司 一种分级反应复合脱硫塔
CN204841409U (zh) * 2015-07-21 2015-12-09 武汉凯迪电力环保有限公司 高效渐变分级复合脱硫塔

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3410109C3 (de) * 1984-03-20 1993-12-02 Bischoff Gasreinigung Vorrichtung zur nassen Entschwefelung von Rauchgasen
US5928615A (en) * 1996-07-12 1999-07-27 Mcdermott Technology, Inc. Wet scrubber oxidation air sparger arrangement
US6187278B1 (en) * 1998-09-08 2001-02-13 Marsulex Environmental Technologies, Llc Process for controlling ammonia slip in the reduction of sulfur dioxide emission
EP1707875A1 (de) * 2005-03-18 2006-10-04 Lurgi Lentjes AG Rauchgasreinigungsvorrichtung mit verbesserter Oxidationseinrichtung im Waschflüssigkeitssumpf
AU2008357629B2 (en) * 2008-06-13 2015-09-03 Sigan Peng Washing device and washing method for marine exhaust flue gases
US8440006B2 (en) * 2009-08-21 2013-05-14 Alstom Technology Ltd System and method for flue gas scrubbing
US8795416B2 (en) * 2009-10-12 2014-08-05 Babcock & Wilcox Power Generation Group, Inc. Segregated in-situ forced oxidation wet flue gas desulfurization for oxygen-fired fossil fuel combustion
US9457316B2 (en) * 2012-07-12 2016-10-04 The Babcock & Wilcox Company Method for controlling compounds and conditions in a wet flue gas desulfurization (WFGD) unit
CN203090748U (zh) * 2013-03-18 2013-07-31 广州市天赐三和环保工程有限公司 一种用于脱硫塔的氧化空气供应装置

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN2546068Y (zh) * 2001-03-29 2003-04-23 许开天 喷射态顺流组合型板式化工塔器
CN2568291Y (zh) * 2002-09-09 2003-08-27 华东理工大学 多功能脱硫塔
CN2705221Y (zh) * 2004-05-21 2005-06-22 四川乐山禹伽茶业科技开发有限公司 一种自吸式条形泡罩蒸馏塔
CN201669053U (zh) * 2010-05-17 2010-12-15 上海申川环保科技有限公司 设有烟气水洗构件的脱硫装置
CN103623682A (zh) * 2013-12-16 2014-03-12 张继惟 一种用于烟气净化的hc-lscr／o-as工程系统
CN104107628A (zh) * 2014-07-10 2014-10-22 中国神华能源股份有限公司 一种烟气脱硫设备及其方法
CN204469533U (zh) * 2015-01-28 2015-07-15 华能国际电力股份有限公司 一种分级反应复合脱硫塔
CN204841409U (zh) * 2015-07-21 2015-12-09 武汉凯迪电力环保有限公司 高效渐变分级复合脱硫塔

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106621722A (zh) * 2017-02-16 2017-05-10 山东神华山大能源环境有限公司 一种用于湿法脱硫塔内的浆液隔离装置及脱硫塔
CN106902629A (zh) * 2017-05-03 2017-06-30 无锡翱翔环保机械有限公司 脱硫塔环形布水装置
CN109806754B (zh) * 2017-11-21 2024-02-09 国电环境保护研究院有限公司 一种脱硫吸收塔装置
CN109806754A (zh) * 2017-11-21 2019-05-28 国电环境保护研究院有限公司 一种脱硫吸收塔装置
CN108211749A (zh) * 2018-03-28 2018-06-29 李文 一种湿法脱硫喷淋塔及脱硫方法
CN108211749B (zh) * 2018-03-28 2023-12-08 李文 一种湿法脱硫喷淋塔及脱硫方法
CN110530162B (zh) * 2018-07-13 2024-04-16 韶关市力高机械制造有限公司 应用于冲天炉的除尘系统
CN110530162A (zh) * 2018-07-13 2019-12-03 韶关市力高机械制造有限公司 应用于冲天炉的除尘系统
CN109173667B (zh) * 2018-09-25 2023-10-13 内蒙古弘睿节能科技有限公司 一种全自动三级脱硫除尘装置
CN109173667A (zh) * 2018-09-25 2019-01-11 内蒙古弘睿节能科技有限公司 一种全自动三级脱硫除尘装置
CN109200718B (zh) * 2018-09-28 2023-10-24 国能龙源环保有限公司 湿法脱硫除尘系统及其自动冲洗、布水和补水控制方法
CN109200718A (zh) * 2018-09-28 2019-01-15 北京国电龙源环保工程有限公司 湿法脱硫除尘系统及其自动冲洗、布水和补水控制方法
CN109432974B (zh) * 2018-12-25 2024-01-30 武汉森源蓝天环境科技工程有限公司 一种鼓泡式自动循环湿法烟气脱硫装置
CN109432974A (zh) * 2018-12-25 2019-03-08 武汉森源蓝天环境科技工程有限公司 一种鼓泡式自动循环湿法烟气脱硫装置
CN109453641A (zh) * 2018-12-29 2019-03-12 西安科技大学 煤矿井下超声波雾化除硫装置
CN109453641B (zh) * 2018-12-29 2023-12-19 西安科技大学 煤矿井下超声波雾化除硫装置
CN110433594A (zh) * 2019-09-12 2019-11-12 佛山市顺德区东波环保设备有限公司 一种脱硫脱硝环保烟气处理用反应塔
CN110433594B (zh) * 2019-09-12 2024-03-22 佛山市顺德区东波环保设备有限公司 一种脱硫脱硝环保烟气处理用反应塔
CN116059752A (zh) * 2023-02-03 2023-05-05 江苏申正建设工程有限公司 一种烟气除尘脱硫塔及除尘脱硫工艺

Also Published As

Publication number Publication date
US10143957B2 (en) 2018-12-04
US20180140991A1 (en) 2018-05-24

Similar Documents

Publication Publication Date Title
WO2017012557A1 (zh) 一种高效渐变分级复合脱硫塔
CN103908879B (zh) 一种双循环文氏棒塔烟气除尘脱硫系统
CN104607017B (zh) 一种h型烟气除尘脱硫塔及烟气脱硫工艺
JP2015073990A (ja) 湿式脱硫スプレー塔用の方法および装置
RU2149050C1 (ru) Каплеотбойник для движущихся с высокими скоростями газов и повторного нагрева скрубберных газов
CN105617821A (zh) 一种实现超低排放的脱硫除尘的组合工艺
CN101861199A (zh) 多级式烟气脱硫喷淋塔
CN104607021B (zh) 双循环烟气除尘脱硫塔及烟气脱硫方法
CN105381703A (zh) 一种进行湿法烟气脱硫的鼓泡塔及方法
CN104607009B (zh) 烟气除尘脱硫塔及烟气脱硫方法
CN109966879A (zh) 硫磺焚烧后尾气钠法深度脱硫控碱的方法和装置
JP2004533923A (ja) ガスから二酸化硫黄を分離する方法および装置
CN106237825A (zh) 扰流捕捉器及一种湿法烟气脱硫除尘吸收塔
CN105688610A (zh) 一种具有自动排污功能的动力波洗涤塔及其洗涤方法
CN104607022B (zh) 一种h型烟气除尘脱硫反应器及烟气脱硫方法
CN101306319A (zh) 直排式烟气处理方法
CN206008453U (zh) 扰流捕捉器及一种湿法烟气脱硫除尘吸收塔
CN104607013B (zh) H型烟气除尘脱硫塔及烟气脱硫工艺
CN104607020B (zh) 烟气除尘脱硫反应器及烟气脱硫方法
CN104607008B (zh) 一种双循环烟气除尘脱硫塔及烟气脱硫方法
CN108686492B (zh) 烟气除尘脱硫塔及除尘脱硫方法
CN202460462U (zh) 一种用于烧结机烟气脱硫的筛板塔
CN104607019B (zh) 双循环烟气除尘脱硫反应器及烟气脱硫方法
CN104607011B (zh) 一种双循环烟气除尘脱硫反应器及烟气脱硫方法
CN208406602U (zh) 一种炭素厂烟气的脱硫装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16827248

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 15577046

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 16827248

Country of ref document: EP

Kind code of ref document: A1