WO2016050030A1 - 旋汇耦合超净脱硫除尘一体化系统及其脱硫除尘方法 - Google Patents

旋汇耦合超净脱硫除尘一体化系统及其脱硫除尘方法 Download PDF

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Publication number
WO2016050030A1
WO2016050030A1 PCT/CN2015/072843 CN2015072843W WO2016050030A1 WO 2016050030 A1 WO2016050030 A1 WO 2016050030A1 CN 2015072843 W CN2015072843 W CN 2015072843W WO 2016050030 A1 WO2016050030 A1 WO 2016050030A1
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Prior art keywords
flue gas
slurry
flow
dust removal
tube
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PCT/CN2015/072843
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English (en)
French (fr)
Inventor
张开元
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北京国电清新环保技术股份有限公司
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Priority to CN201580016531.2A priority Critical patent/CN106457140B/zh
Priority to KR1020167031394A priority patent/KR101932091B1/ko
Priority to CA2960532A priority patent/CA2960532C/en
Priority to MYPI2017700422A priority patent/MY187496A/en
Priority to BR112017003845-5A priority patent/BR112017003845B1/pt
Priority to EP15845727.5A priority patent/EP3202483B1/en
Application filed by 北京国电清新环保技术股份有限公司 filed Critical 北京国电清新环保技术股份有限公司
Priority to US15/315,367 priority patent/US9915423B2/en
Priority to JP2017513293A priority patent/JP6461319B2/ja
Priority to AU2015327602A priority patent/AU2015327602B2/en
Publication of WO2016050030A1 publication Critical patent/WO2016050030A1/zh
Priority to PH12017500206A priority patent/PH12017500206A1/en
Priority to HK17105895.6A priority patent/HK1232183A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • 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
    • 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
    • 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
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/608—Sulfates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

Definitions

  • the invention relates to an integrated system and method for ultra-clean desulfurization and dust removal, in particular to an integrated system and method for deep desulfurization, dust removal and defogging of flue gas containing sulfur dioxide and dust.
  • the cyclone tower in the field of boiler flue gas desulfurization has the following problems: due to the short gas-liquid contact time on the tray, the desulfurization efficiency is low, both are about 80%, and it is not suitable for CaCO 3 as a sulfur-fixing agent. Moreover, the structure is complicated, the scale is easy to be scaled, and the desulfurization efficiency decreases as the tower diameter increases. The cyclone tower is tangentially inlet, and the center is easy to form an inefficient zone. To this end, the industry has developed a spin-off desulfurization technology, which is an upgrade technology based on pneumatic emulsification technology. Pneumatic emulsification technology is suitable for flue gas desulfurization of small boilers.
  • the flue gas desulfurization technology mostly adopts the empty tower technology, that is, the flue gas enters the absorption tower and does not pass through the device, and directly reacts with the slurry sprayed on the upper portion. In this way, the flue gas and the slurry will be short-circuited, and some of the flue gas will leave the absorption tower without reacting, and the flue gas residence time is short, resulting in low desulfurization efficiency.
  • wet desulfurization generally adopts empty tower spray technology.
  • a larger liquid-gas ratio and multi-layer spray are required.
  • even double towers are required to meet the requirements.
  • the bias flow of the flue gas after entering the absorption tower is an unavoidable problem.
  • the dust removal and defogging process routes of flue gas are various, but the dehumidification and defogging of saturated wet flue gas containing a large number of droplets at the same time, especially the high-efficiency deep dust removal and defogging, the technical route and process equipment are relatively small. .
  • the “demister + wet electric dust removal” process route or the “GGH+ bag dust removal” process route can be adopted, which can effectively reduce the dust pollution discharge.
  • both processes have certain defects.
  • the efficiency of the desulfurization system needs to be increased from 97.5% to 98%, and the SO 2 concentration in the net flue gas of the absorption tower outlet needs to be reduced from 50mg/Nm 3 to 40mg/Nm 3 to meet the emission requirements, if the air leakage during the GGH operation is considered As the rate increases, the desulfurization efficiency of the absorption tower needs to be further improved. Therefore, this process has no practical significance in China.
  • the present invention provides a cyclone coupled ultra-clean desulfurization and dust removal integrated system and a method thereof for optimizing the existing desulfurization technology, enhancing the desulfurization effect, and avoiding the deficiencies of the existing dust removal and defogging technologies.
  • the utility model has the advantages of simple structure, reliable operation, obvious effect, stable operation, low energy consumption and low cost, and can realize deep desulfurization, dust removal and defogging of flue gas, and achieve ultra-clean emission.
  • the guide tube is a circular tube placed vertically.
  • the angle between the blade of the turbulent and the central cylinder is 20 degrees to 55 degrees, and the shielding ratio between adjacent blades is -10% to 45%.
  • the blade inclination angle satisfies an actual speed of gas rotation movement of the gas after the blade is guided by ⁇ 8 m/s.
  • central cylinder is a circular cylinder whose top end is closed, and the cross-sectional area thereof is 15% to 50% of the cross section of the draft tube.
  • the thickness and height of the water retaining ring are determined to obtain a maximum liquid holding capacity.
  • the tube bundle type dust removing and mist removing device has a flushing water assembly distributed to each dust removing and defogging unit, and the flushing water assembly is disposed on a center axis of the draft tube of the dust removing and defogging unit, and the flushing water assembly includes a flushing nozzle The flushing nozzle is perpendicular to the inner wall of the draft tube.
  • the utility model relates to a cyclone coupling ultra-clean desulfurization and dust removal integrated desulfurization and dust removal method, which is applied to the above-mentioned integrated system of the cyclone coupling ultra-clean desulfurization and dust removal, comprising the following steps:
  • Step 1 Oxidation of the slurry and gypsum crystallization
  • Oxidizing air is introduced into the slurry tank, and the oxidizing air is thoroughly mixed with the limestone-gypsum slurry under the action of the agitator to oxidize calcium sulfite in the slurry component to calcium sulfate, and the calcium sulfate crystallizes into gypsum particles;
  • the swirling vane in the cyclone coupling device causes the flue gas in the tower to change from the bottom to the upward direction and accelerates it; the spray layer sprays the slurry, and the slurry flowing from the top to the bottom is in contact with the flue gas, and some flue gas is present. Converging to the center, under the constraint of narrowing the inner diameter of the flow guiding device, the flue gas and the slurry in the upward swirling flow are turned into a confluence, and the slurry falls back to the center, and rapid desulfurization and slurry washing are performed to remove part of the dust;
  • the flue gas running at high speed enters the tube bundle type dust removing and demisting device, and the turbulent part in the lower part of the dust removing and defogging device causes a large amount of droplet liquid particles and dust particles in the flue gas to collide with each other to agglomerate into larger particles and settle down;
  • Step 6 Deep dust removal and defogging
  • the rapid cooling and uniform flue gas action of the gas-liquid cyclone coupling device can reduce the formation of water mist and the entrainment of dust in the flue gas while reducing the desulfurization effect, and reduce the load of subsequent defogging and dust removal;
  • Tube bundle dust removal and defogging device has good effect and low running resistance, which can replace the conventional “defogger + wet electric dust removal” process, providing a new reliable and cheap process for dust removal and defogging of saturated flue gas.
  • FIG. 3 is a schematic structural view of a dust removing and defogging unit of the present invention.
  • Figure 4 is a schematic view showing the structure of a swirler and a swirling cylinder of the present invention.
  • Figure 6 is a schematic diagram of a turbulent flow of the present invention.
  • the slurry is transported from the absorption tower slurry tank to the slurry spray layer by a slurry circulation pump. Between the swirl coupling device and the spray layer, the flue gas is from bottom to top, and the slurry is from top to bottom, gas and liquid.
  • countercurrent contact in which the concentration gradient of reactants and products is large, is conducive to the progress of the positive reaction, and can reduce the sulfur dioxide content in the original flue gas and the concentration of calcium sulfite in the slurry after desulfurization as much as possible, and the desulfurization effect is good.
  • the cyclone coupling device has the function of uniformly distributing flue gas, and when the flue gas enters the cyclone coupling device, the swirling vanes of each unit are rotated toward the swirling cylinder wall, and at the same time The slurry flowing from the spray layer partially contacts the center after contact with the flue gas.
  • the swirling vane causes turbulence of the slurry and the flue gas, thereby increasing the gas-liquid mass transfer effect.
  • the flue gas and the slurry swirl upward.
  • the inner diameter of the flow guiding device becomes narrow, so that the flue gas becomes a confluence, and the slurry is blocked from falling downward.
  • a gas-liquid mass transfer system with a large gas-liquid rotation, overturning and turbulence is generated in the space of the cyclone coupling device, in which the gas-liquid-solid three-phase is fully contacted,
  • the gas-liquid membrane mass transfer resistance is reduced and the mass transfer rate is increased.
  • the flue gas effectively completes the desulfurization process in the above space and removes part of the dust.
  • the slurry absorbs sulfur dioxide and then falls back into the slurry tank to form a by-product gypsum.
  • the cyclone coupling device has the function of rapidly cooling the flue gas.
  • the main working principle of the tube bundle type dust removing and demisting device of the invention is that the three motion states of the droplet liquid particles and the dust solid particles are agglomeration, trapping and quenching, respectively.
  • the agglomeration means that when the flue gas passes through the device, the fine mist droplets are mixed with each other, and between the droplet liquid particles and the dust particles collide and form a larger particle in the high-speed moving airflow in the device.
  • a cyclone coupled ultra-clean desulfurization and dust removal integrated system includes a spray layer 3 installed in the tower body 1, a slurry tank 5 disposed at a lower portion of the tower body 1, and installed in the slurry tank 5 for circulation.
  • the pump 6, the screw coupling device 4 and the tube bundle type dust removing and demisting device 2 are installed in the upper portion of the slurry tank 5 and the lower portion of the spray layer 3, and the tube bundle type dust removing and mist removing device 2 is disposed at the top of the tower body 1.
  • the cyclone coupling device 4 includes a plurality of screw coupling units 41 and a support beam 42 for fixing at a lower portion of the screw coupling unit, and adjacent spiral coupling units are connected by a sealing plate 46, as shown in FIG. .
  • Each of the cyclocoupling coupling units includes a swirling cylinder 44, a swirling cylinder is provided with a swirler 43, and a swirling cylinder top is mounted with a flow guiding device 45.
  • the swirl 43 includes an inner cylinder 431 and a swirl vane 432.
  • the inner diameter of the flue gas outlet of the flow guiding device 45 is smaller than the inner diameter of the inlet of the flue gas, and the inner diameter is narrowed by the width to make the passing flue gas reach the confluence effect.
  • the cross-section of the flow guiding device 45 may be trapezoidal, as shown in Figure 5a; it may also be an inverted bowl shape, as shown in Figure 5b; or a hyperbolic shape, as shown in Figure 5c
  • the cyclone coupling device 4 is installed between the original flue gas inlet of the absorption tower and the spray layer 3.
  • the slurry sprayed by the spray layer 3 flows through the cyclone coupling device 4 to the absorption tower slurry tank, and the original flue gas is thoroughly mixed with the spray slurry when passing through the screw coupling device 4, and is cooled and cooled, washed, absorbed, and then sprayed.
  • the cyclone coupling device 4 is composed of a plurality of screw coupling units 41 uniformly arranged on the tower body section, and the single swirl coupling unit 41 is composed of a swirler 43, a swirling cylinder 44 and a flow guiding device 45,
  • the convolution coupling units 41 are combined by a closing plate 46 into a convolution coupling device 4 covering the entire absorption tower section.
  • the weight of the screw coupling device 4 is borne by the support beam 42.
  • the slurry sprayed by the spray layer 3 continuously enters the swirl coupling unit 41 through the flow guiding device 45, and the swirling flow increases as the amount of slurry in the swirl coupling unit 41 increases.
  • the slurry in the upper portion of the sub-43 is not continuously maintained, and a portion of the slurry near the lower end of the cyclone 43 is discharged from the cyclone coupling unit 41 and falls back into the slurry tank 5.
  • the dust removing and defogging unit further includes a water retaining ring 23 for forming a liquid film layer having a certain stable liquid amount in the dust removing and defogging unit;
  • the water retaining ring 23 is an annular member having a thickness and a height, and is attached Attached to the inner wall of the draft tube 21, it is a component for controlling the liquid holding capacity of the dust removing and defogging unit.
  • the thickness and height parameters of the water retaining ring 23 are set to obtain the maximum liquid holding capacity of the dust removing and defogging unit.
  • the tube bundle type dust removing and demisting device further includes a plurality of bleed holes 24 for controlling a wall surface of the draft tube 21 to form a liquid film layer having a uniform thickness at a high speed; the bleed hole 24 is a blade 222.
  • the opening is the same in the direction of rotation, and is tangential to the inner wall portion of the draft tube 21.
  • the tube bundle type dust removing and demisting device has a flushing water assembly distributed to each unit, and the flushing water assembly is disposed on a central axis of the guiding tube 21 of the dust removing and defogging unit, the flushing water assembly includes a flushing nozzle, and the flushing nozzle is perpendicular to the guide The inner wall of the flow tube.
  • the guide tube 21 is a flue gas overflowing member of the tube bundle type dust removing and demisting device 2, and is a circular tube having a closed inner wall surface which is smooth and flat and has no closed ends.
  • the average cross section of the exhaust pipe of the guide tube 21 The flow rate is between 2 and 8 m/s, and the residence time in the average guide tube is 0.1 to 0.5 s.
  • the flue gas inlet at the bottom of the draft tube 21 and the middle of the draft tube 21 are each placed with a turbulent 22.
  • the guiding of the turbulence 22 is to provide a dynamic environment for the removal of droplets and dust.
  • the turbulent part 22 is an air flow guiding member that changes the over-current flue gas from the top-down moving direction to the high-speed rotating motion, and is composed of a central cylinder 221 and a vane 222. In order to ensure high dust removal and defogging efficiency, two layers of turbulents are generally used.
  • the blade 222 is a sheet-like curved segment-shaped member having a smooth surface, which is evenly distributed at an oblique angle in an annular region between the central cylinder 221 and the draft tube 21, and the angle between the blade 222 and the central cylinder 221 is 20 to 55. Degree, the blocking ratio between adjacent blades is -10% to 45%.
  • the angle between the swirl vane 432 of the swirl 43 and the inner cylinder 431, and the blocking ratio between the vane 432 and the adjacent swirl vane 432 may be the same as or different from the vane 222 of the choke 22.
  • the number, inclination angle and coverage area of the blades 222 can be adjusted according to the inlet dust content.
  • the inclination angle of the blade 222 is also related to the overcurrent speed of the guide tube 21.
  • the central cylinder 221 is a circular cylinder with an outer smooth closed top end, the diameter of which is related to the diameter of the draft tube 21, and generally the cross-sectional area of the central cylinder 221 is 15% to 50% of the cross section of the draft tube.
  • Two water retaining rings are disposed in the guide tube 21, and the water retaining ring is a component for controlling the liquid holding capacity of the dust removing and demisting device, and the primary water retaining ring 231 is disposed under the upper turbulent 22, twice A water retaining ring 232 is disposed at the outlet of the draft tube 21.
  • the venting hole 24 is a component of the dust removing and defrosting device 2 for controlling the thickness of the liquid film on the wall surface of the guiding tube 21, and is the same as the rotating direction of the blade 222, and is tangential to the inner wall surface of the draft tube 21, and the slit is smooth.
  • limestone-gypsum wet desulfurization The liquid droplets are derived from two parts, one part is a fine slurry droplet generated by the collision of the spray slurry, and the other part is a fine mist formed by the condensation of the saturated net flue gas; the dust solid particles contained in the net flue gas also have two components. Part of it is fine dust particles that are not captured by the slurry in the flue gas, and some of which are insoluble gypsum and limestone particles suspended in the slurry droplets. These two parts are based on the "dust" under the existing measurement standards.
  • the characteristic of desulfurization and net flue gas is that the flue gas is saturated and low temperature, the mist droplet content is large, and the dust content is large.
  • the droplets and dust in the airflow of the high-speed rotary motion are greatly different from the density of the gas, and gradually start to move toward the wall surface by the centrifugal force. Under the action of the airflow, the accumulated droplets accumulate Then, a rotating liquid film having a uniform thickness is formed on the wall surface of the draft tube 21, and the rotation direction of the liquid film is the same as that of the air flow.
  • the mist and the dust approach the wall surface of the draft tube 21 at a high speed, the liquid film is contacted with the rotating liquid film.
  • the liquid film absorbs and quenches.
  • the film thickness is insufficient or there is no liquid film.
  • the liquid film When the liquid film is at a certain height, it is blocked by the water retaining ring 23, and the liquid film is broken and scattered to fall into the upper part of the turbulent 22, forming a huge number of droplets in the cavity of the dust removing and defogging unit, and entering the dust removing and defogging.
  • the flue gas contact of the unit realizes the capture of the mist and the dust, and is thrown to the liquid film with the high-speed airflow, and then the liquid film is re-dispersed into droplets by the water retaining ring 23.
  • the rotating liquid film repeatedly washes the wall surface of the draft tube 21, effectively preventing the fouling of the gypsum crystal.
  • the surface of the blade 222 is flushed by a high-speed airflow, and the minimum pitch of the blade is also 20 mm or more, so there is no problem of fouling and clogging.
  • the airflow continues to move upward, the angular velocity of the rotation gradually begins to decrease, and some of the finer droplets and dust have not been removed.
  • a turbulent 22 is placed, and the highly rotating environment of the airflow is repeatedly repeated.
  • the process of removing droplets and dust from condensation, capture and annihilation finally achieves the purification of mist and dust in the flue gas.
  • the running resistance of the tube bundle type dust removing and demisting device 2 is only 350 Pa, and the removal effect can satisfy the dust emission concentration of 5 mg/Nm 3 at the outlet.
  • the tube bundle type dust removing and demisting device 2 is made of high-strength PP material, has light weight and low cost, and meets corrosion resistance and structural strength requirements.
  • the flow rate of the running flue gas is larger than the flue gas flow rate of the absorption tower section, and can be directly placed in the absorption tower, and the arrangement is simple and convenient.
  • the number of dust removal and defogging units depends on the flow rate of the flue gas at the outlet of the tower body 1.
  • the number of dust removal and defogging units is designed according to the flow rate of the over-flowing flue gas in each unit of the unit of 2000 to 2500 m 3 .
  • the integrated cyclodesulfurization and dust removal integrated desulfurization and dust removal method of the invention comprises slurry spraying and circulation, gas-liquid cyclone coupling contact and reaction, slurry oxidation and gypsum crystallization, tube bundle dust removal and removal of outlet flue gas fog.
  • the original flue gas enters the desulfurization absorption tower body 1 through the induced draft fan or the booster fan, and passes through the cyclone coupling device 4, the spray layer 3, and the tube bundle type dust removing and demisting device 2 from bottom to top, after the desulfurization and dust removal purification is completed. Finally, it is discharged into the chimney through the net flue.
  • the high-temperature raw flue gas After entering the absorption tower, the high-temperature raw flue gas firstly mixes and mixes with the slurry sprayed by the swirling coupling device 4 and the spray layer 3, and realizes preliminary purification under the action of cooling, washing and absorption of the slurry, and the temperature of the original flue gas is lowered.
  • the working pressure of the nozzle is 0.04 ⁇ 0.1MPa, the average droplet size of the spray droplet is ⁇ 2mm, and the ratio of liquid to gas is between 5 and 20.
  • the temperature of the flue gas at this time Further cooling, wherein the water vapor concentration reaches a saturated state, and the flue gas leaves the spray layer 3, except for the fine dust remaining in the original raw flue gas which is not caught by the droplet coupling device 4 and the spray layer 3 droplets.
  • the flue gas after desulfurization enters the tube-type dust removing and demisting device 2 at a speed of the average flow velocity of the absorption tower section of 2 to 6 m/s, and is also in the fine slurry droplets and flue gas in the tube bundle type dust removing and demisting device 2
  • the remaining dust is caught and removed, and the total amount of dust at the outlet of the bundle-type dust removal and defogging device 2 is controlled below 5 mg/Nm 3 , and the flue gas is thoroughly purified into clean flue gas, which is discharged into the chimney through the outlet flue of the absorption tower. emission.
  • the dust and slurry droplets caught by the tube-type dust removal and demisting device 2 are separated from the tube-type dust removal and demisting device 2, and flow into the absorption tower 5 at the lowermost part of the absorption tower under gravity, and remain in the bundle-type dust removal and defogging.
  • the dust and slurry inside the device 2 are cleaned regularly by the tube bundle type dust removing and demisting device flushing water assembly; the flushing water of the tube bundle type dust removing and demisting device 2 is provided by the tube bundle type dust removing and demisting device, the flushing water pump extracting process water, and the flushing water working head 0.1 to 0.4 MPa.
  • the invention relates to a cyclone coupled ultra-clean desulfurization and dust removal integrated desulfurization and dust removal method, which is applied to the above-mentioned ultra-clean desulfurization and dust removal integrated system, and comprises the following steps:
  • Step 1 Oxidation of the slurry and gypsum crystallization
  • Oxidized air is introduced into the slurry tank 5, and the oxidizing air is sufficiently mixed with the limestone-gypsum slurry under the action of the agitator to oxidize the calcium sulfite in the slurry component to calcium sulfate, and the calcium sulfate crystallizes into gypsum particles.
  • Step 2 Spraying and circulation of the slurry
  • the slurry containing the slurry obtained in the first step is pumped into the multi-layer spray layer 3 by a circulation pump, and sprayed.
  • the slurry is returned to the slurry tank 5.
  • the nozzle working pressure of the spray layer 3 is 0.04 to 0.1 MPa, the average droplet size of the spray droplets is ⁇ 2 mm, and the liquid-gas ratio is between 5 and 20.
  • the swirling vane 432 is used to change the direction of the flue gas flow from the bottom to the top in the tower, so that the flue gas is turned from the vertical upward to the upward direction and accelerated, and the flue gas contacts the slurry sprayed by the spray layer 3 to remove the SO 2 and Part of the dust is converged toward the center of the cyclone coupling unit 41 by the inner diameter of the deflector 45.
  • the slurry mixed with the flue gas falls under the blocking of the flow guiding device 45, and falls back to the upper portion of the swirler 43.
  • the flue gas obtains a higher rotation speed under the action of the swirling vane 432.
  • the linear velocity of the flue gas particle is about 10-15 m/s, and the velocity field distribution gradually decreases from the center to the edge along the swirl vane, and the velocity vector direction is along the swirling flow.
  • the blade rotates upward in the oblique direction; the high-speed airflow is mixed with a large amount of slurry, and the airflow is dispersed into a plurality of small bubbles.
  • the slurry is also driven by the high-speed airflow to rotate at a high speed in the cyclone coupling device, and the maximum rotational linear velocity of the slurry can be reached.
  • the flue gas in the cyclone coupling device, can complete the mixing, contact and reaction with the slurry under the condition of the average flow velocity of the section of about 2-6m/S, and the rotation velocity of the slurry in the cyclone coupling device and
  • the amount of slurry decreases as the average cross-sectional flow rate decreases, but the average contact time of the flue gas with the slurry increases as the average flow velocity of the section decreases.
  • the amount of time in which the gas-liquid two phases of the flue gas and the slurry in the cyclone coupling device are mixed, contacted, and reacted is about 0.2 to 0.5 s.
  • Step 4 Preliminary dust removal and defogging
  • the flue gas after desulfurization enters the tube bundle type dust removing and demisting device 2 at a speed of the average flow velocity of the absorption tower section of 2 to 6 m/s, forming droplet liquid particles and dust particles, and utilizing the turbulence provided in the lower part of the dust removing and defogging unit.
  • Sub 22 combines the droplet liquid particles with the dust particles to form a larger particle settling.
  • the average flow velocity of the cross-flow flue gas section of the guide tube 21 is 2-8 m/s, and the residence time of the average diversion cylinder is 0.1-0.5 S.
  • Step 5 Further dust removal and defogging
  • the flue gas continues to move at a high speed, and the droplet liquid particles are in full contact with the dust solid particles, and the liquid catches the separation.
  • the net flue gas moves upwards uniformly with a large amount of mist and dust at a flow rate of 3.5 m/s, and enters the tube bundle type dust removal and demisting device 2 area.
  • the flow velocity increases to 5 m/s.
  • the flow velocity of the gas flow increases to above 8 m/s, and the gas flow direction changes from vertical upward to rotational upward.
  • the turbulence intensity of the airflow is greatly enhanced.
  • the probability of collision between the droplets and dust in the net flue gas in the severe turbulent gas phase is greatly increased, so that the droplets are condensed into larger droplet particles to achieve partial removal.
  • Step 6 Deep dust removal and defogging
  • step 5 further dedusting and defogging the flue gas
  • the droplet liquid particles and the dust solid particles rotate with the flue gas
  • the droplets and dust in the air stream rotating at high speed are greatly different due to the density of the gas, and gradually become the centrifugal force.
  • a layer of rotating liquid film having a uniform thickness is formed on the inner wall surface of the guide tube 21 after the accumulated droplets are accumulated.
  • the rotation direction of the liquid film is the same as that of the airflow, and when the droplets and dust are close to the wall surface at a high speed state, After contact with the rotating liquid film, it is absorbed and quenched by the liquid film.
  • the running resistance of the tube bundle type dust removing and demisting device 2 is 350 Pa, and the removal effect satisfies the dust emission concentration of 5 mg/Nm 3 at the outlet, and the droplet content reaches 25 mg/Nm 3 or less.

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Abstract

一种旋汇耦合超净脱硫除尘一体化系统及其脱硫除尘方法，该系统包括喷淋层（3）、浆池（5）和循环泵，还包括旋汇耦合装置（4）和管束式除尘除雾装置（2），旋汇耦合装置（4）安装在浆池（5）上部、喷淋层（3）下部，管束式除尘除雾装置（2）设置在塔体（1）顶部，旋汇耦合装置（4）包括多个旋汇耦合单元（41）和位于其下部用于固定的支撑梁（42），每个旋汇耦合单元（41）包括旋流筒（44）、旋流子（43）、导流装置（45），旋流子（43）包括内筒体（431）和旋流叶片（432），导流装置（45）烟气流出处的内径小于烟气流入处的内径；管束式除尘除雾装置（2）包括多个除尘除雾单元，每个除尘除雾单元包括导流筒（21）和n个设置在导流筒（21）内的湍流子（22），湍流子（22）均垂直于导流筒（21）壁上下布置。

Description

旋汇耦合超净脱硫除尘一体化系统及其脱硫除尘方法 技术领域
本发明涉及一种超净脱硫除尘一体化系统和方法，具体地说，涉及一种对含二氧化硫及粉尘的烟气进行深度脱硫、除尘、除雾的一体化系统和方法。
背景技术
目前在锅炉烟气脱硫领域的旋流器塔存在下列问题：由于塔板上的气液接触时间短，因此脱硫效率偏低，均为80％左右，且不适用于CaCO3作固硫剂，并且结构复杂，容易结垢，且脱硫效率随塔径增加而降低。旋流器塔为切向进气，中心容易形成低效区。为此业界开发了旋汇脱硫技术，该技术是在气动乳化技术基础上的升级技术。气动乳化技术适用于小型锅炉的烟气脱硫，该技术在放大实验中存在明显的放大效应，存在一定局限性。且目前烟气脱硫技术多采用空塔技术，即烟气进入吸收塔后不经过该装置，直接与上部喷淋的浆液进行反应。这样烟气和浆液就会短路，一些烟气没有反应就离开了吸收塔，且烟气停留时间短，造成脱硫效率低。
湿法烟气净化的主要工作是脱硫，但是为了改善净烟气对环境的影响，对其中的粉尘(包括石膏)和液滴的要求也越来越严格，所以要研究深度的脱硫、除尘、除雾技术。
目前，湿法脱硫一般都是采用空塔喷淋技术，为了达到较高的脱硫效率，需要较大的液气比和多层喷淋，对一些提效改造项目甚至需要双塔串联以满足要求。另外，由于烟道和吸收塔尺寸以及结构的特殊性，烟气进入吸收塔后的偏流是一个不能避免的问题。
烟气的除尘、除雾工艺路线多种多样，但对含有大量雾滴的饱和湿烟气同时实现除尘、除雾，尤其是高效深度除尘除雾的可选技术工艺路线和工艺设备均比较少。
目前，国内现有的大型燃煤锅炉烟气95％以上采用湿法脱硫工艺，外排低温饱和净烟气中含有石膏浆液和尘，且基本上均未配置GGH，造成严重的“石膏雨”现象和尘污染排放量较大。造成这种问题的主要原因在于除雾器仅能脱除粒径大于15μm以上的较大液滴，因此烟气中含有的大量细小浆液雾滴造成净烟气中排放尘含量较高。
对于现有的湿法脱硫净烟气的脱尘除雾工艺，可以采用“除雾器+湿式电除尘”工艺路线，或采用“GGH+布袋除尘”工艺路线，可有效降低尘污染的排放量。但此两种工艺均存在一定缺陷。
采用“GGH+布袋除尘”工艺路线时，由于GGH和布袋除尘器的运行阻力巨大，建设成本也较高，更重要的是由于GGH存在一定的漏风率，这对于脱硫系统的脱硫效果影响巨大。我国的大气污染排放标准中SO2的排放浓度要求严格，均在50mg/Nm3以下，而绝大部分燃煤烟气中SO2浓度均在2000mg/Nm3以上，以GGH漏风率0.5％计，则需要脱硫系统的效率从97.5％增加到98％,吸收塔出口净烟气中的SO2浓度需要从50mg/Nm3降低至40mg/Nm3才能满足排放要求，如果考虑GGH运行过程中漏风率增加，吸收塔的脱硫效率还需进一步提高。因此，此工艺在我国无实际应用的意义。
采用“除雾器+湿式电除尘”工艺路线时，可以保证对吸收塔出口净烟气的高效脱尘除雾效果，可出口尘含量小于5mg/Nm3。目前此工艺仅应用在少数新建脱硫吸收塔上，主要原因在于湿式电除尘设备重量、体积巨大，只有新建吸收塔按此工艺路线设计时才能实现。另外，此工艺路线由于利用高压电场捕悉雾滴和粉尘颗粒，其设备中有很多高压电气设备，电极线均为高级合金材质构成，其建造成本高昂，运行电耗大，也是限制其应用的原因之一。在已建项目脱硫塔上进行工艺路线改造升级难以实现的原因主要在于，原吸收塔的结构设计强度无法满足电除尘器的荷载需要；相邻布置时场地面积的需求也限制了其外置布置的可能性，再加上相邻布置时增加的巨大运行 阻力，造成此工艺路线的运行成本进一步上升。由于有大量的高压电气设备，此工艺路线的运行维护复杂，对运行操作的技术要求高，运行维护成本较高。
发明内容
为解决上述问题，本发明提供了一种旋汇耦合超净脱硫除尘一体化系统及其脱硫除尘方法目的在于优化现有脱硫技术，增强脱硫效果，避免现有除尘、除雾技术的不足，其构造简单，运行可靠、效果明显，运行稳定，能耗小，成本较低，能实现烟气的深度脱硫、除尘和除雾，达到超净排放。具体技术方案如下：
一种旋汇耦合超净脱硫除尘一体化系统，包括安装在塔体中的喷淋层、设置在塔体下部的浆池，安装在浆池中循环泵，旋汇耦合装置和管束式除尘除雾装置，旋汇耦合装置安装在浆池上部、喷淋层下部，管束式除尘除雾装置设置在塔体顶部，其中，
所述旋汇耦合装置包括多个旋汇耦合单元和位于所述旋汇耦合单元下部用于固定的支撑梁，相邻的旋汇耦合单元之间用密封板连接，每个所述旋汇耦合单元包括旋流筒，旋流筒内设有旋流子，旋流筒顶部设有导流装置，旋流子包括内筒体和旋流叶片，所述导流装置烟气流出处的内径小于烟气流入处的内径；
所述管束式除尘除雾装置包括多个除尘除雾单元，每个所述除尘除雾单元包括导流筒和n个设置在所述导流筒内的湍流子，n≥1；所述n个湍流子均垂直于导流筒壁上下布置。
进一步，所述的导流筒为垂直放置的圆形筒。
进一步，所述导流筒的数量、直径和高度根据下列参数确定：当出口尘含量≤5mg/Nm3时，导流筒过流烟气断面平均流速为5～6m/s,停留时间为0.2～0.3S。
进一步，所述的湍流子包括若干叶片均匀分布在中心筒外壁和导流筒内 壁之间的环状区域内。
进一步，所述湍流子的叶片与中心筒夹角为20度～55度，相邻叶片之间的遮挡率为-10％～45％。
进一步，所述的叶片倾斜角度满足气体经叶片导向后气体旋转运动的实际速度≥8m/s。
进一步，所述中心筒为顶端封闭的圆形筒，其截面面积为导流筒截面的15％～50％。
进一步，所述管束式除尘除雾装置的导流筒内壁上设有挡水环，用于形成含有稳定液体量的液膜层。
进一步，所述的挡水环的厚度和高度，以获得最大持液量确定。
进一步，所述管束式除尘除雾装置设有泄放孔，用于控制装置内壁面形成一个高速旋转的厚度均匀的液膜层；所述泄放孔为与叶片旋转方向相同的，与导流筒内壁面部分相切的开孔。
进一步，所述的管束式除尘除雾装置具有分配到每个除尘除雾单元的冲洗水组件，冲洗水组件设置在除尘除雾单元的导流筒中心轴线上，所述冲洗水组件包括冲洗喷嘴，冲洗喷嘴垂直于导流筒内壁。
一种旋汇耦合超净脱硫除尘一体化脱硫除尘方法,应用于上述的一种旋汇耦合超净脱硫除尘一体化系统，包括以下步骤：
步骤一：浆液的氧化和石膏结晶
在浆池内通入氧化空气，在搅拌器的作用下氧化空气与石灰石-石膏浆液充分混合，使所述浆液成分中的亚硫酸钙氧化为硫酸钙，硫酸钙结晶为石膏颗粒；
步骤二：浆液的喷淋和循环
根据原烟气的条件和对净烟气的要求，采用循环泵将步骤一中所述的浆液抽入多层喷淋层进行喷淋；
步骤三：气液的旋汇耦合接触和反应
旋汇耦合装置中的旋流叶片使在塔内由下向上的烟气改变流向并且使其加速；喷淋层喷淋浆液，自上而下流下的浆液与烟气接触后，有部分烟气向中心汇流，受导流装置内径变窄的约束继续旋流向上的烟气与浆液变成汇流，浆液向中心回落，进行快速脱硫和浆液洗涤脱除部分粉尘；
步骤四：初步除尘和除雾
高速向上运行的烟气进入管束式除尘除雾装置，除尘除雾装置下部的湍流子使烟气中的大量雾滴液体颗粒与粉尘颗粒，相互碰撞而凝聚成较大的颗粒后沉降下来；
步骤五：进一步除尘和除雾
管束式除尘除雾装置内的液膜层与继续高速向上运动的烟气雾滴液体颗粒与粉尘固体颗粒充分接触后，液体捕悉实现分离；
步骤六：深度除尘和除雾
继续高速向上运动的烟气雾滴液体颗粒与粉尘固体颗粒随烟气高速旋转，利用与烟气的密度差实现离心分离，被抛向管束式除尘除雾装置导流筒内壁表面，与装置壁面附着的液膜层接触后湮灭。
本发明的有益效果是：
1.系统脱硫效果好，效率可以达到99％以上，出口二氧化硫含量可达30mg/Nm3以下，运行阻力稍有增加，但是可以减少喷淋层和浆液循环泵的配置，总体上不会增加能耗；
2.系统除尘、除雾效果好，出口尘含量可达5mg/Nm3以下，液滴含量可达25mg/Nm3以下；
3.系统无结垢堵塞风险，冲洗水量小，冲洗频率低；
4.系统运行可靠，安装方便，维护简单，效果好，造价低，性价比高；
5.气液旋汇耦合装置的快速降温和均布烟气作用，在提高脱硫效果的同时，可以减少烟气中水雾的形成和尘的夹带，减轻后续除雾、除尘的负荷；
6.管束式除尘、除雾装置效果好，运行阻力低，可替代常规的“除雾器+湿式电除尘”工艺，为饱和烟气的脱尘除雾提供一种新的可靠、廉价的工艺设备选择；
7.在改造项目上，可拆除原有的普通除雾器直接安装管束式除尘、除雾装置，增加阻力约100～150Pa，不产生其他运行消耗。
附图说明
图1为本发明的系统组成示意图；
图2为本发明的旋汇耦合装置结构示意图；
图3为本发明的除尘除雾单元的结构示意图；
图4为本发明的旋流子和旋流筒的结构示意图；
图5a-5c为本发明的导流装置截面示意图；
图6为本发明的湍流子示意图；
图中标号分别代表：
1-塔体，2-管束式除尘除雾装置，3-喷淋层，4-旋汇耦合装置，5-浆池，41-旋汇耦合单元，42-支撑梁，43-旋流子，44-旋流筒，45-导流装置，46-封闭板，431-内筒体，432-旋流叶片，21-导流筒，22-湍流子，23-挡水环，24-泄放孔，221-中心筒，222-叶片，231-一次挡水环，232-二次挡水环。
具体实施方式
以下结合附图对发明的原理和特征进行描述，所举实例只用于解释本发明，并非用于限定本发明的范围。
本发明是将钙法脱硫的常规技术与气液的旋汇耦合和管束式除尘除雾 技术相结合，将浆液的喷淋和循环、气液的旋汇耦合接触和反应、浆液的氧化和石膏结晶、出口烟气的管束式除尘和除雾四部分，有机的组合在一个脱硫吸收塔内，形成一种旋汇耦合超净脱硫除尘的一体化方法和系统，从下往上脱硫、除尘效果逐渐加强，最终在管束式除尘除雾装置中，除雾的作用加强了除尘的效果。
在整个脱硫过程中，浆液是用浆液循环泵由吸收塔浆池输送到浆液喷淋层，在旋汇耦合装置和喷淋层间，烟气由下往上，浆液由上往下，气液总体上逆流接触，其中的反应物和产物浓度梯度较大，有利于正反应的进行，可以尽可能的降低原烟气中的二氧化硫含量和脱硫后浆液中亚硫酸钙的浓度，脱硫效果好。
本发明的旋汇耦合装置的主要工作原理：旋汇耦合装置具有均布烟气的作用，当烟气进入旋汇耦合装置后，被其各个单元的旋流叶片旋向旋流筒壁，同时从喷淋层流下的浆液与烟气接触后有部分向中心汇流。旋流叶片对浆液和烟气造成湍流作用，从而增加气液传质效果。烟气与浆液旋流向上，当达到导流装置的出口时，由于导流装置内径变窄，使得烟气变成汇流，浆液受阻向下回落。通过旋流和汇流的耦合多相紊流掺混，在旋汇耦合装置空间内造成一个气液旋转、翻覆、湍流度很大的气液传质体系，在其中气液固三相充分接触，气液膜传质阻力降低，传质速率提高。烟气在上述空间内有效的完成脱硫过程，并脱除了部分粉尘。浆液吸收二氧化硫后回落入浆池生成副产物石膏排出。另外，所述旋汇耦合装置具有使烟气快速降温的作用。
本发明的管束式除尘除雾装置的主要工作原理：雾滴液体颗粒与粉尘固体颗粒的三种运动状态分别为凝聚、捕悉和湮灭。所述凝聚是指烟气经过装置时，其中夹杂的细小的雾滴液体颗粒相互之间，雾滴液体颗粒与粉尘颗粒之间，在装置中高速运动的气流中碰撞而凝聚成较大的颗粒后沉降下来；所述捕悉是指雾滴液体颗粒与未脱除的粉尘固体颗粒跟随气体进入装置，与该 装置内导流筒上具有一定稳定液体量的液膜层充分接触后，被液体捕悉实现从烟气中分离出来，进入液膜层；所述湮灭是指雾滴液体颗粒与未脱除的粉尘固体颗粒，随烟气在装置内高速旋转，利用与烟气的密度差实现离心分离，被抛向导流筒内壁表面，与该导流筒内壁表面高速旋转的、厚度均匀的液膜层接触后湮灭。所述的管束式除尘除雾装置具有再次均布烟气的作用。
如图1所示，一种旋汇耦合超净脱硫除尘一体化系统，包括安装在塔体1中的喷淋层3，设置在塔体1下部的浆池5，安装在浆池5中循环泵6，旋汇耦合装置4和管束式除尘除雾装置2，旋汇耦合装置4安装在浆池5上部、喷淋层3下部，管束式除尘除雾装置2设置在塔体1顶部。
旋汇耦合装置4包括多个旋汇耦合单元41和位于所述旋汇耦合单元下部用于固定的支撑梁42，相邻的旋汇耦合单元之间用密封板46连接，如图2所示。每个所述旋汇耦合单元包括旋流筒44、旋流筒设有旋流子43、旋流筒顶部安装导流装置45。旋流子43包括内筒体431和旋流叶片432。所述导流装置45烟气流出处的内径小于烟气流入处的内径，内径由宽变窄使通过的烟气达到汇流的效果。导流装置45的截面可以是梯形，如图5a所示；也可以是倒扣的碗形，如图5b所示；或者是双曲线形，如图5c所示。
旋汇耦合装置4安装在吸收塔原烟气入口与喷淋层3之间。喷淋层3喷淋的浆液通过旋汇耦合装置4流至吸收塔浆池，原烟气通过旋汇耦合装置4时与喷淋浆液充分混合接触，降温冷却、洗涤、吸收反应后进入喷淋层3；旋汇耦合装置4由多个旋汇耦合单元41在塔体断面上均匀排布组成，单个旋汇耦合单元41由旋流子43、旋流筒44和导流装置45组成，多个旋汇耦合单元41通过封闭板46组合成一个覆盖整个吸收塔断面的旋汇耦合装置4。旋汇耦合装置4的重量由支承梁42承担。
烟气通过旋汇耦合装置4时，在旋流子43的作用下，气流与旋流子43上部高速旋转运动的浆液发生剧烈碰撞，气流被分散成数量众多的细小气泡 混合在浆液中，同时高速运动的气流为浆液提供持续不断的旋转动力；细小的气泡与浆液的充分混合促使烟气快速降温，气液的两相膜接触面积的增加促进了气液的传质效果，原烟气中的SO2被浆液吸收反应，烟气中夹带的尘也被洗涤；旋转运动中的气泡与旋流子43上部的旋转浆液在旋流筒44内逐渐向上运动，在导流装置45的阻挡下，浆液流跌落返回旋流子43上部，而气体穿过导流装置45继续向上运动进入喷淋层3；均匀分布的多个旋汇耦合单元41将穿过旋汇耦合装置4的原烟气均匀的分布在整个吸收塔断面上，喷淋层3喷淋的浆液不断通过导流装置45进入旋汇耦合单元41内，随着旋汇耦合单元41内的浆液量的增加，旋流子43上部的浆液无法持续保持，一部分靠近旋流子43下端的浆液便排出旋汇耦合单元41，回落入浆池5内。
管束式除尘除雾装置2包括多个除尘除雾单元。如图3所示，每个所述除尘除雾单元包括导流筒21和n个设置在所述导流筒内的湍流子22，n≥1；所述n个湍流子22均垂直于导流筒21壁上下布置。导流筒21为垂直放置的圆形筒。除尘除雾单元内还包括挡水环23，用于在除尘除雾单元内形成具有一定稳定液体量的液膜层；所述的挡水环23为具有厚度和高度的环状部件，其贴附在导流筒21内壁上，是除尘除雾单元控制持液量的部件。挡水环23的厚度和高度参数的设定，以获得除尘除雾单元的最大持液量为准。
如图3所示，管束式除尘除雾装置还包括多个泄放孔24，用于控制导流筒21内壁面形成一个高速旋转的厚度均匀的液膜层；泄放孔24为与叶片222旋转方向相同，与导流筒21内壁面部分相切的开孔。管束式除尘除雾装置具有分配到每个单体的冲洗水组件，冲洗水组件设置在除尘除雾单元的导流筒21中心轴线上，所述冲洗水组件包括冲洗喷嘴，冲洗喷嘴垂直于导流筒内壁。
导流筒21为管束式除尘除雾装置2的烟气过流部件，是一个垂直放置的内壁面光滑平整的两端无封闭的圆形筒。导流筒21的过流烟气断面平均 流速在2～8m/s,平均导流筒内停留时间0.1～0.5S。
导流筒21底部的烟气进口和导流筒21中部，各放置一件湍流子22。所述的湍流子22导向作用是为雾滴与粉尘的脱除提供动力环境。所述的湍流子22是脱尘除雾装置2过流烟气从自上而下的运动方向转变为高速旋转运动的气流导向部件，由中心筒221和叶片222组成。为了保证较高的脱尘除雾效率，一般采用两层湍流子。
叶片222是一个表面光滑的薄片状曲扇形部件，它以一定倾斜角度均匀分布在中心筒221与导流筒21之间的环形区域内所述叶片222与中心筒221夹角为20度～55度，相邻叶片之间的遮挡率为-10％～45％。旋流子43的旋流叶片432与内筒体431的夹角，以及该叶片432与相邻旋流叶片432之间的遮挡率，可以与湍流子22的叶片222的相同，也可以不同。叶片222的数量、倾斜角度与覆盖面积根据入口尘含量需要可以进行调整，通常原烟气入口尘含量越高，叶片的数量越多，倾斜角度越小，覆盖面积越大。同时叶片222倾斜角度与导流筒21的过流速度也有关系，导流筒21的过流速度越大，叶片222的倾斜角度越大；叶片角度满足气体经叶片导向后气体旋转运动的实际速度≥8m/s。
中心筒221为一个外部光滑的顶端封闭的圆形筒，其直径与导流筒21的直径相关，通常中心筒221的截面面积为导流筒截面的15％～50％。
在所述的导流筒21内设置两个挡水环，所述的挡水环是脱尘除雾装置控制持液量的部件，一次挡水环231设置在上部湍流子22下，二次挡水环232设置在导流筒21出口处。
挡水环的厚度和高度参数影响着装置的运行阻力。挡水环厚度、高度在合理数值时可获得装置的最大持液量，此时捕悉作用大大加强，运行阻力也大大增加，因此挡水环参数应该与烟气中雾滴总量、雾滴粒径分布、粉尘的粒径和特性等综合考虑。
在所述的导流筒21上，下部湍流子22上一定高度设置二排泄放孔24，二排泄放孔24均匀的间布在同一的断面上。泄放孔24与导流筒21内壁相切，方向与叶片222旋转方向相同。下排泄放孔24孔径大于上排泄放孔24孔径，泄放孔24的数量与孔径的大小根据烟气进口雾滴含量调整。所述的泄放孔24为脱尘除雾装置2控制导流筒21壁面液膜厚度的部件，是一个与叶片222旋转方向相同的，与导流筒21内壁面部分相切的，切口光滑平整的开孔。所述的泄放孔24的大小、数量和布置高度与与烟气中雾滴总量、雾滴粒径分布、粉尘的粒径和特性等有关。放泄孔24要保证被装置脱除的雾滴与尘被及时从装置中排出，避免液膜变厚造成二次雾滴产生，还要避免排出液体过多无法维持液膜，高速运动的雾滴、粉尘直接与装置导流筒21内壁碰撞造成更大量更细小的二次雾滴粉尘产生。
以典型的含有大量雾滴需要脱尘除雾处理的石灰石-石膏湿法脱硫净烟气为例描述管束式除尘除雾装置2的运行如下：石灰石-石膏湿法脱硫净烟气中含有的雾滴液体颗粒来源于两部分，一部分是喷淋浆液相互碰撞产生的细小浆液液滴，一部分是饱和净烟气降温冷凝生成的细小雾滴；净烟气中含有的粉尘固体颗粒也有两个组成，一部分是烟气中未被浆液捕悉的细小粉尘固体颗粒，一部分是浆液液滴中悬浮的不溶性石膏、石灰石颗粒，这两部分在现有的测量标准下均以“尘”计。脱硫净烟气的特点就是烟气饱和低温，雾滴含量大，尘含量大。
净烟气带着大量的雾滴和粉尘向上运动，进入管束式除尘除雾装置2区域。穿过一级湍流子22后，气体流向从垂直向上变化为旋转向上，此时气流的紊流强度大大加强。净烟气中的雾滴、粉尘在剧烈的紊流气相中相互碰撞机率大幅增加，从而凝聚成较大的液滴颗粒实现了部分脱除。
高速旋转运动的气流中的雾滴和粉尘由于与气体的密度差异巨大，在离心力的作用下逐渐开始向壁面方向运动。在气流的作用下，捕悉的液滴积聚 后在导流筒21壁面上形成一层厚度均匀的旋转液膜，液膜的旋转方向与气流相同，雾滴和粉尘以高速状态靠近导流筒21壁面时，与旋转的液膜接触后被液膜吸收湮灭。液膜厚度不足或无液膜，高速运动的雾滴和粉尘直接撞击在壁面上势必生成更为细小的雾滴和粉尘，无法达到除雾除尘的目的。液膜厚度过大，高速运动的气流会将液膜表面的液体切削吹散成为雾滴。吸收了雾滴和粉尘的液膜旋转运动到放泄孔24位置时，部分液膜便从放泄孔24中排出装置，从而达到稳定液膜厚度的目的。
液膜在一定高度上时受到挡水环23的阻挡，液膜被破坏散落成液滴跌落返回湍流子22上部，在除尘除雾单元空腔内形成数量巨大的液滴，与进入除尘除雾单元的烟气接触，实现对雾滴和粉尘的捕悉，并随着高速气流被抛向液膜，再由挡水环23将此部分液膜重新散落成液滴。
旋转的液膜反复冲刷导流筒21壁面，有效防止石膏结晶的结垢堵塞问题。叶片222表面有高速气流冲刷，叶片间距最小处也有20mm以上，因此也不存在结垢堵塞问题。
气流随着继续向上运动，旋转的角速度逐渐开始降低，而部分更为细小的雾滴与粉尘还未能被脱除，此时再设置一个湍流子22，重复给予气流的高度旋转的环境，重复凝聚、捕悉和湮灭的雾滴、粉尘脱除过程，最终达到实现对烟气中雾滴和粉尘的净化。管束式除尘除雾装置2的运行阻力仅350Pa，脱除效果可满足出口5mg/Nm3的尘排放浓度。
所述管束式除尘除雾装置2采用高强度PP材质制造，重量轻，成本低，满足耐腐蚀和结构强度要求。其运行烟气流速大于吸收塔断面烟气流速，可直接安置在吸收塔内，布置简单方便。
旋汇耦合装置中的旋汇耦合单元41数量取决于系统过流气体的工况流量的大小。一般旋汇耦合单元41数量按照每个单元单位小时内过流烟气工况流量2～2.5万m3设计；烟气通过旋汇耦合装置4和喷淋层3后SO2被脱除， 烟气温度也降至饱和温度，此时的烟气的工况流量下降。
除尘除雾单元数量取决于塔体1出口的烟气工况流量，除尘除雾单元数量按照每个单元单位小时内过流烟气工况流量2000～2500m3设计。
除尘除雾单元数a与旋汇耦合单元数量b在入口烟气为饱和烟气时的比例关系为a:b＝9～10:1；当入口烟气为不饱和烟气时，除尘除雾单元数a与旋汇耦合单元数量b的比例为a:b＝5～9:1。
实施例
本发明的旋汇耦合超净脱硫除尘一体化脱硫除尘方法，包括浆液的喷淋和循环、气液的旋汇耦合接触和反应、浆液的氧化和石膏结晶、出口烟气的管束式除尘和除雾。原烟气经引风机或增压风机进入脱硫吸收塔塔体1内，自下而上依次通过旋汇耦合装置4、喷淋层3、管束式除尘除雾装置2，完成脱硫除尘净化后，最终通过净烟道排入烟囱排放。高温原烟气在进入吸收塔后首先在旋汇耦合装置4与喷淋层3喷淋下来的浆液充分混合接触，在浆液的冷却、洗涤、吸收作用下实现初步净化，原烟气温度降低，大部分的SO2在此处得到脱除，并有部分尘在旋汇耦合装置4内被浆液洗涤捕悉下来；旋汇耦合装置4出口的烟气通过喷淋层3时，与喷淋层3喷淋液滴逆向接触，实现进一步的脱硫，使得管束式除尘除雾装置2入口的SO2浓度进一步降低至35mg/Nm3以下；喷淋层3的喷淋浆液来源于吸收塔浆池5的浆液经过浆液循环泵加压后通过喷淋层喷嘴喷射，喷嘴工作压力0.04～0.1MPa，喷淋液滴平均粒径～2mm，液气比在5～20之间；此时的烟气温度被进一步降温，其中的水蒸汽浓度达到饱和状态，烟气离开喷淋层3时除含有剩余的原烟气中未被旋汇耦合装置4和喷淋层3液滴捕悉的微尘外，还夹带着一部分喷淋层产生的细小浆液液滴；脱硫后的烟气以吸收塔断面平均流速2～6m/s的速度进入管束式除尘除雾装置2内，在管束式除尘除雾装置2内细小的浆液液滴和烟气中还存留的微尘被捕悉脱除，管束式除尘除雾装置2出口的尘总量被 控制在5mg/Nm3以下，烟气被彻底净化为洁净烟气，通过吸收塔出口烟道排入烟囱排放。管束式除尘除雾装置2捕悉的尘、浆液液滴汇聚后脱离管束式除尘除雾装置2，在重力作用下流入吸收塔最下部的吸收塔浆池5中，残留在管束式除尘除雾装置2内部的尘和浆液由管束式除尘除雾装置冲洗水组件定期冲洗清楚；管束式除尘除雾装置2的冲洗水由管束式除尘除雾装置冲洗水泵抽取工艺水提供，冲洗水工作压头0.1～0.4MPa。
本发明的一体化超净脱硫除尘系统，在满足更加严格的环保要求前提下，投资成本和运行成本较低，便于新旧脱硫系统的建设和改造。
本发明提出的一种旋汇耦合超净脱硫除尘一体化脱硫除尘方法,应用于上述的超净脱硫除尘一体化系统，包括以下步骤：
步骤一：浆液的氧化和石膏结晶
在浆池5内通入氧化空气，在搅拌器的作用下氧化空气与石灰石-石膏浆液充分混合，使所述浆液成分中的亚硫酸钙氧化为硫酸钙，硫酸钙结晶为石膏颗粒。
步骤二：浆液的喷淋和循环
根据原烟气的条件和对净烟气的要求(5mg/Nm3的尘排放浓度)，采用循环泵将步骤一中获得的含有浆液抽入多层喷淋层3进行喷淋，喷淋后的浆液回到浆池5。喷淋层3的喷嘴工作压力为0.04～0.1MPa，喷淋液滴平均粒径～2mm，液气比在5～20之间。
步骤三：气液的旋汇耦合接触和反应
利用旋流叶片432改变塔内由下向上的烟气流向，使烟气由垂直向上变成旋转向上并且使其加速，烟气与喷淋层3喷淋后的浆液接触，脱除SO2和部分尘，受导流装置45内径由宽变窄的约束向旋汇耦合单元41中心汇流。与烟气混合后的浆液在导流装置45的阻挡下，跌落返回旋流子43上部。烟气在旋流叶片432的作用下获得较高的旋转速度，烟气质点线速度约 10-15m/s，速度场分布沿旋流叶片从中心至边缘逐渐降低，速度矢量方向为沿旋流叶片倾斜方向旋转向上运动；高速气流与大量的浆液剧烈混合，气流被分散成众多细小气泡，浆液在高速气流的推动下也在旋汇耦合装置内高速旋转运动，浆液的最高旋转线速度可达5m/s；在旋汇耦合装置内，烟气在断面平均流速约2-6m/S条件下均能很好的完成与浆液的混合、接触、反应，旋汇耦合装置内的浆液旋转流速和浆液量随着平均断面流速的下降而减少，但烟气与浆液的平均接触时间随断面平均流速的降低而增加。旋汇耦合装置内烟气与浆液的气液两相混合、接触、反应的时间量约为0.2～0.5S。
步骤四：初步除尘和除雾
步骤三中脱硫后的烟气以吸收塔断面平均流速2～6m/s的速度进入管束式除尘除雾装置2内，形成雾滴液体颗粒与粉尘颗粒，利用设在除尘除雾单元下部的湍流子22，将所述雾滴液体颗粒与粉尘颗粒凝聚成较大的颗粒沉降。导流筒21的过流烟气断面平均流速在2～8m/s,平均导流筒内停留时间为0.1～0.5S
步骤五：进一步除尘和除雾
经过步骤四初步除尘和除雾继续高速向上运动的烟气，雾滴液体颗粒与粉尘固体颗粒充分接触，液体捕悉实现分离。
净烟气带着大量的雾滴和粉尘以3.5m/s的流速均匀向上运动，进入管束式除尘除雾装置2区域。烟气进入管束式除尘除雾装置2时的流速增加到5m/s，穿过一级湍流子22后，气流的质点流速增加到8m/s以上，气体流向从垂直向上变化为旋转向上，此时气流的紊流强度大大加强。净烟气中的雾滴、粉尘在剧烈的紊流气相中相互碰撞机率大幅增加，从而凝聚成较大的液滴颗粒实现了部分脱除。
步骤六：深度除尘和除雾
经过步骤五进一步除尘和除雾的烟气，雾滴液体颗粒与粉尘固体颗粒随 烟气旋转，高速旋转运动的气流中的雾滴和粉尘由于与气体的密度差异巨大，在离心力的作用下逐渐开始向壁面方向运动。在气流的作用下，捕悉的液滴积聚后导流筒21内壁面上形成一层厚度均匀的旋转液膜，液膜的旋转方向与气流相同，雾滴和粉尘以高速状态靠近壁面时，与旋转的液膜接触后被液膜吸收湮灭。吸收了雾滴和粉尘的液膜旋转运动到放泄孔24位置时，部分液膜从放泄孔24中排出。管束式除尘除雾装置2的运行阻力为350Pa，脱除效果满足出口5mg/Nm3的尘排放浓度，液滴含量达到25mg/Nm3以下。
以上所述仅为本发明的较佳组合实施举例，并不用以限制本发明，凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (12)

  1. 一种旋汇耦合超净脱硫除尘一体化系统，包括安装在塔体中的喷淋层、设置在塔体下部的浆池和安装在浆池中循环泵，其特征在于，还包括旋汇耦合装置和管束式除尘除雾装置，旋汇耦合装置安装在浆池上部、喷淋层下部，管束式除尘除雾装置设置在塔体顶部，其中，
    所述旋汇耦合装置包括多个旋汇耦合单元和位于所述旋汇耦合单元下部用于固定的支撑梁，相邻的旋汇耦合单元之间用密封板连接，每个所述旋汇耦合单元包括旋流筒，旋流筒内设有旋流子，旋流筒顶部设有导流装置，旋流子包括内筒体和旋流叶片，所述导流装置烟气流出处的内径小于烟气流入处的内径；
    所述管束式除尘除雾装置包括多个除尘除雾单元，每个所述除尘除雾单元包括导流筒和n个设置在所述导流筒内的湍流子，n≥1；所述n个湍流子均垂直于导流筒壁上下布置。
  2. 如权利要求1所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述的导流筒为垂直放置的圆形筒。
  3. 如权利要求1或2所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述导流筒的数量、直径和高度根据下列参数确定：当出口尘含量≤5mg/Nm3时，导流筒过流烟气断面平均流速为5～6m/s,停留时间为0.2～0.3S。
  4. 如权利要求1所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述的湍流子包括若干叶片均匀分布在中心筒外壁和导流筒内壁之间的环状区域内。
  5. 如权利要求4所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述湍流子的叶片与中心筒夹角为20度～55度，相邻叶片之间的遮挡率为-10％～45％。
  6. 如权利要求4或5所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述的叶片倾斜角度满足气体经叶片导向后，气体旋转运动的实际速度≥8m/s。
  7. 如权利要求4所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述中心筒为顶端封闭的圆形筒，其截面面积为导流筒截面的15％～50％。
  8. 如权利要求1所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述管束式除尘除雾装置的导流筒内壁上设有挡水环，用于形成含有稳定液体量的液膜层。
  9. 如权利要求8所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述的挡水环的厚度和高度，以获得最大持液量确定。
  10. 如权利要求1所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述管束式除尘除雾装置设有泄放孔，用于控制装置内壁面形成一个高速旋转的厚度均匀的液膜层；所述泄放孔为与叶片旋转方向相同的，与导流筒内壁面部分相切的开孔。
  11. 如权利要求1所述的旋汇耦合超净脱硫除尘一体化系统，其特征在于，所述的管束式除尘除雾装置具有分配到每个除尘除雾单元的冲洗水组件，冲洗水组件设置在除尘除雾单元的导流筒中心轴线上，所述冲洗水组件包括冲洗喷嘴，冲洗喷嘴垂直于导流筒内壁。
  12. 一种旋汇耦合超净脱硫除尘一体化脱硫除尘方法,其特征在于，包括以下步骤：
    步骤一：浆液的氧化和石膏结晶
    在浆池内通入氧化空气，在搅拌器的作用下氧化空气与石灰石-石膏浆液充分混合，使所述浆液成分中的亚硫酸钙氧化为硫酸钙，硫酸钙结晶为石膏颗粒；
    步骤二：浆液的喷淋和循环
    根据原烟气的条件和对净烟气的要求，采用循环泵将步骤一中所述的浆液抽入多层喷淋层进行喷淋；
    步骤三：气液的旋汇耦合接触和反应
    旋汇耦合装置中的旋流叶片使在塔内由下向上的烟气改变流向并且使其加速；喷淋层喷淋浆液，自上而下流下的浆液与烟气接触后，有部分烟气向中心汇流，受导流装置内径变窄的约束继续旋流向上的烟气与浆液变成汇流，浆液向中心回落，进行快速脱硫和浆液洗涤脱除部分粉尘；
    步骤四：初步除尘和除雾
    高速向上运行的烟气进入管束式除尘除雾装置，除尘除雾装置下部的湍流子使烟气中的大量雾滴液体颗粒与粉尘颗粒，相互碰撞而凝聚成较大的颗粒后沉降下来；
    步骤五：进一步除尘和除雾
    管束式除尘除雾装置内的液膜层与继续高速向上运动的烟气雾滴液体颗粒与粉尘固体颗粒充分接触后，液体捕悉实现分离；
    步骤六：深度除尘和除雾
    继续高速向上运动的烟气雾滴液体颗粒与粉尘固体颗粒随烟气高速旋转，利用与烟气的密度差实现离心分离，被抛向管束式除尘除雾装置导流筒内壁表面，与装置壁面附着的液膜层接触后湮灭。
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