WO2020001258A1 - 一种烟气脱硫脱硝除尘脱白装置 - Google Patents

一种烟气脱硫脱硝除尘脱白装置 Download PDF

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Publication number
WO2020001258A1
WO2020001258A1 PCT/CN2019/090487 CN2019090487W WO2020001258A1 WO 2020001258 A1 WO2020001258 A1 WO 2020001258A1 CN 2019090487 W CN2019090487 W CN 2019090487W WO 2020001258 A1 WO2020001258 A1 WO 2020001258A1
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Prior art keywords
flue gas
absorption tower
denitration
dust removal
tower
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PCT/CN2019/090487
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English (en)
French (fr)
Inventor
胡小吐
胡静龄
钟璐
杨颖欣
刘勇
薛学良
Original Assignee
广东佳德环保科技有限公司
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Priority claimed from CN201810688458.9A external-priority patent/CN108554145A/zh
Priority claimed from CN201821019928.4U external-priority patent/CN208493775U/zh
Application filed by 广东佳德环保科技有限公司 filed Critical 广东佳德环保科技有限公司
Publication of WO2020001258A1 publication Critical patent/WO2020001258A1/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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes

Definitions

  • the present application relates to the technical field of flue gas treatment, for example, to a flue gas desulfurization, denitration, dust removal and whitening device.
  • a large number of pollutants (such as SO 2 , NO x , heavy metals, dioxins, VOCs, PM, etc.) released during the combustion of fuel are the main reasons for the increasingly deteriorating environment, and the purification of flue gas after combustion is an effective way to control pollution emissions one.
  • Aiming at flue gas desulfurization and denitrification, coal-fired power plants at home and abroad currently widely use the technology combination of NH 3 selective catalytic reduction (NH 3 -SCR) denitration and wet flue gas desulfurization (WFGD). Although this technology combination has high desulfurization and denitrification efficiency, it is not suitable for the treatment of sintering of steel and some industrial boilers and other furnaces.
  • flue gas dewhitening is also required, but the related flue gas dewhitening method has a complicated system structure. It is necessary to increase the temperature and the energy consumption, which is not conducive to energy saving and emission reduction.
  • Wet desulfurization, denitrification and whitening can not only eliminate smog pollution, but also achieve low-cost environmental protection standards, ultra-low near-zero emissions, annual water saving potential of billions of tons, and can take into account the contradiction between environment and development.
  • CN107983078A discloses a de-whitening and zero-emission system that integrates the functions of cooling water cooling and electrostatic trapping of liquid droplets to solve the problem of white smoke bands generated during the desulfurization process in the wet desulfurization process. Its cooling is achieved by heat exchange of cooling water pipes. The use of electric fields to capture liquid droplets with static electricity consumes a large amount of power, and the overall structure is more complex, and the amount of smoke suitable for processing is small.
  • CN107781832A discloses a coal-fired wet desulfurization flue gas dehydration and reheating waste heat utilization and discharge system.
  • the waste heat recovery and utilization in the flue gas can be realized.
  • the sprayed flue gas is subjected to spray cooling and dehydration treatment to recover the latent heat released by the flue gas; the sprayed flue gas is subjected to heat treatment by the flue gas heater and discharged to the atmosphere. And after the spray is cooled and then heated and discharged, the humidity in the flue gas may be increased during this spraying process, and the effect of whitening may be reduced.
  • the related technology still lacks a flue gas purification technology that has a wide range of applications, integrated desulfurization, denitrification, and whitening, and can simultaneously remove multiple pollutants.
  • the purpose of this application is to provide a flue gas desulfurization, denitrification, dust removal, and whitening device, which has a wide range of applications, integrated desulfurization, denitrification, and whitening, can simultaneously remove a variety of pollutants, and has a low device cost and continuous and stable operation.
  • a flue gas desulfurization, denitration, dust removal and whitening device is provided with a dust collector, a fan, a primary absorption tower, a secondary absorption tower, a pretreatment washing tower, a wet electrostatic precipitator, and a dust collector, which are sequentially connected through a flue gas pipe along the direction of flue gas movement.
  • the dust collector is provided with a flue gas inlet
  • the top of the chimney is provided with a flue gas outlet
  • the water washing tower is connected to the cooling tower through a water pipe.
  • the flue gas generated by the factory is initially dusted by a dust collector, and then sent to a first-level absorption tower through a fan.
  • the first-level absorption tower is desulfurized and denitrated by means of spraying agents.
  • the spraying layer of the first-level absorption tower has multiple layers.
  • the leaching agent is an alkaline agent, which can be removed by chemical reaction with sulfide and nitrate. After the first-stage absorption of the flue gas, it then enters the second-stage absorption tower to spray and absorb it for deep desulfurization and denitrification.
  • the flue gas enters the pretreatment water washing tower and is directly contacted with the flue gas by circulating cooling water Reduce the temperature, cool the flue gas to below 45 degrees Celsius, reduce the water content in the saturated flue gas, circulating cooling water circulates between the pretreatment water washing tower and the cooling tower. After cooling water is cooled in the pretreatment water washing tower to absorb the heat from the flue gas, The heat is released in the cooling tower to cool down, and then recycled to the pretreatment water washing tower for recycling. After the flue gas has cooled down, it enters a wet electrostatic precipitator to further remove moisture from the aerosol and flue gas, and then is discharged through the flue gas outlet at the top of the chimney.
  • the first core of this application is to further reduce the flue gas temperature through water cooling.
  • the color of the flue gas easily turns white because the temperature of the flue gas discharged from the flue gas outlet is about 60 ° C, which is much higher than the outdoor environment temperature of 10-30 ° C.
  • the temperature of the flue gas is lowered after mixing with the atmosphere. The amplitude is large.
  • water vapor will condense, and the residual sulfide in the flue gas will react with water to form sulfurous acid.
  • the sulfurous acid is unstable and is easily oxidized to form small droplets of sulfuric acid. That is, "white smoke".
  • the present application inputs cooling water through a cooling tower, so that the flue gas is circulated and washed in the water washing tower, and the circulating cooling water is directly contacted with the flue gas to cool down, and the flue gas can be cooled below 45 degrees Celsius.
  • the temperature of the flue gas at the outlet is reduced by 10-15 degrees Celsius, which can greatly reduce the "white smoke". It has been proved in practice that the "white smoke" can be reduced by more than 60-90%.
  • the method further includes a first ozone dosing and uniformizing device provided between the fan and the first-stage absorption tower, and a first ozone-feeding uniformizer provided between the first-stage absorption tower and the second-stage absorption tower.
  • the second ozone dosing and spreading device is connected between the first ozone dosing and spreading device and the second ozone dosing and spreading device through an ozone pipe.
  • the second core of the present application is to add ozone to the flue gas.
  • the primary absorption tower and the secondary absorption tower both adopt the technical route of ozone oxidation combined with wet washing, and the strong oxidizing ozone O 3
  • the sulfur oxides and nitrogen oxides are oxidized into high-priced sulfur oxides and nitrogen oxides which are easily absorbed.
  • the sulfur oxides SO x and nitrogen oxides NO x contained in the flue gas react with ozone.
  • the specific reaction formula is as follows:
  • the flue gas enters the washing tower.
  • This application is based on the technical route of ozone oxidation combined with wet washing.
  • the strong oxidizing O 3 is used to oxidize the NO, which is difficult to dissolve in water, to the water-soluble phase.
  • Good high-valence nitrogen oxides (such as NO 2 , NO 3 , N 2 O 5, etc.), so as to achieve the integrated removal of SO 2 and NO x .
  • the first-stage absorption tower is provided with a first-stage absorption tower tray, a first-stage absorption tower spray layer, and a first-stage absorption tower demister in order along the smoke moving direction.
  • the first-level absorption tower spray layer is provided with three spray layers.
  • the primary absorption tower can perform preliminary treatment of sulfur oxides and nitrogen oxides.
  • the secondary absorption tower is provided with a secondary absorption tower tray, a spraying layer under the secondary absorption tower, a filler layer of the secondary absorption tower, and a spraying layer on the secondary absorption tower in this order in the direction of the flue gas movement.
  • two-stage absorption tower demister is provided.
  • the filling layer of the secondary absorption tower is provided between the spraying layer under the secondary absorption tower and the spraying layer on the secondary absorption tower, which can not only absorb the flat airflow and absorb sulfur oxides, nitrogen oxides, but more importantly, make the The spraying layer on the secondary absorption tower and the spraying layer below the secondary absorption tower are washed separately, and the solubility of the slurry between the two washing layers is different, which can more efficiently treat sulfur oxides and nitrogen oxides in the flue gas.
  • the spraying layer below the secondary absorption tower and the spraying layer above the secondary absorption tower are two-layer spraying.
  • a secondary absorption tower is added. Compared with the previous primary absorption, it can deeply process sulfur oxides and nitrogen oxides in flue gas, and has better desulfurization and denitration effects.
  • the pretreatment water washing tower is sequentially provided with a pretreatment water washing tower packing layer, a pretreatment water washing tower spray layer, and a pretreatment water washing tower demister along the direction of flue gas movement.
  • the pretreatment water washing tower is mainly used to cool down the flue gas.
  • the spraying agent of the pretreatment water washing tower comes from the circulating cooling water with the cooling tower. The cost is low, the treatment effect is good, and it can continue to run stably.
  • the secondary absorption tower packing layer is a ceramic packing
  • the pretreatment water washing tower packing layer is a PP (polypropylene) corrugated structured packing.
  • the first-stage absorption tower demister, the second-stage absorption tower demister, and the pretreatment water washing tower demister are all folded plate demisters; as an optional embodiment, all The first-stage absorption tower tray and the second-stage absorption tower tray are both alloy enhancement trays, and the alloy enhancement trays can improve airflow distribution.
  • the first spraying agent of the primary absorption tower is a NaOH solution
  • the second spraying agent used by the secondary absorption tower is a mixed solution of Na 2 SO 3 and NaHCO 3 .
  • the third core of the present application is that the flue gas is washed through two stages of circulation, and the spraying agents used in the first stage absorption tower and the second stage absorption tower are different.
  • NaOH solution is used for simultaneous desulfurization and denitration
  • the reaction between SO 2 and NaOH solution is preferential.
  • SO 2 can react with NaOH quickly and generate SO 3 2- ion, which has a high removal efficiency; but high concentration SO 2 has a certain inhibitory effect on the absorption of NO x in NaOH solution, and the reaction between NO x and NaOH has problems such as low reaction rate and unsatisfactory removal efficiency, so SO 2 in the flue gas can achieve the standard, but It is difficult to guarantee NO x compliance.
  • the first spraying agent is a NaOH solution and the desulfurization product is Na 2 SO 3 .
  • the second spraying agent is prepared by adding NaHCO 3 to the product absorbed by the first spraying agent.
  • the desulfurization product of the first spraying agent can be selected as Na 2 SO 3 , and NaHCO 3 is added as a buffer to prepare the second spraying agent, which can be recycled and save resources. Ozone oxidation combined with two-stage wet washing can achieve more thorough desulfurization and denitrification.
  • the first ozone dosing and spreading device and the second ozone dosing and spreading device are both ozone uniform distribution devices, and the ozone uniform distribution device includes a flue gas pipe and is disposed on the flue gas.
  • the ozone dosing device in the pipeline includes a main air inlet pipe and a plurality of air outlet nozzles provided in the main air inlet pipe.
  • the ozone uniform distribution device further includes a plurality of first units and a plurality of first units provided in the flue gas pipe.
  • Two units a plurality of first units are arranged parallel to each other and spaced apart from each other, a plurality of second units are fixedly connected to a plurality of first units, and the air outlets of the air outlet nozzles are disposed toward the first unit.
  • the first unit is an oval tube
  • the second unit is a keel plate
  • a plurality of concave holes are evenly distributed along the length direction of the oval tube, and the concave holes are directly opposite to the air outlet nozzle.
  • an anticorrosive layer is provided in the recessed hole.
  • the first unit is a first grooved plate
  • the second unit is a second grooved plate
  • a plurality of second grooved plates are in communication with a plurality of first grooved plates.
  • the openings of the profile plate and the second trough profile plate are arranged toward the air outlet of the air outlet nozzle.
  • the opening of the first grooved plate is directly opposite the air outlet of the air outlet nozzle.
  • the symmetrical centerline of the first grooved plate and the gas outlet direction of the gas outlet nozzle form an included angle of 30-60 °.
  • Two-stage circulating washing, and the spraying agents used in the first-stage absorption tower and the second-stage absorption tower are different, which can achieve more suitable desulfurization and denitration.
  • FIG. 1 is a schematic view of a process flow of a device in an embodiment of the present application
  • FIG. 2 is a schematic diagram of an arrangement of an oval tube and a keel plate in Embodiment 1 of the present application;
  • FIG. 3 is a schematic diagram of an arrangement of an oval tube and an ozone dosing device in Embodiment 1 of the present application;
  • FIG. 4 is an enlarged view of a portion A in FIG. 3;
  • FIG. 5 is a schematic diagram of an arrangement of a first trough plate and an ozone dosing device in Embodiment 2 of the present application;
  • FIG. 6 is a schematic layout diagram of a first grooved plate and a second grooved plate in Embodiment 2 of the present application;
  • FIG. 7 is a sectional view of the A-A plane in FIG. 6;
  • FIG. 8 is a schematic diagram of the arrangement of the first trough plate and the ozone doser in the third embodiment of the present application.
  • each reference numeral the technical characteristics indicated by each reference numeral are as follows: 1. Flue gas inlet; 2. Dust collector; 3. Fan; 4. Ozone generator; 5. First ozone dosing and spreader; 6. Primary absorption tower; 601, primary absorption tower tray; 602, primary absorption tower spray layer; 603, primary absorption tower demister; 7, secondary absorption tower; 701, secondary absorption tower tray; 702, Spray layer under secondary absorption tower; 703, secondary absorption tower packing layer; 704, secondary absorption tower spray layer; 705, secondary absorption tower demister; 8, pretreatment water washing tower; 801, pretreatment water washing Tower packing layer; 802, pretreatment water washing tower spray layer; 803, pretreatment water washing tower demister; 9, wet electric dust collector; 10, chimney; 11, cooling tower; 12, flue gas outlet; 13, second Ozone dosing spreader.
  • Primary absorption tower 601, primary absorption tower tray; 602, primary absorption tower spray layer; 603, primary absorption tower demister; 7, secondary absorption tower; 701, secondary absorption tower tray; 702, Spray layer under secondary absorption tower;
  • connection should be understood in a broad sense unless otherwise specified and limited. For example, they may be fixed connections, detachable connections, or mechanical
  • connection can also be an electrical connection, a direct connection, or an indirect connection through an intermediate medium, which can be the internal connection of two elements or the interaction between two elements.
  • intermediate medium can be the internal connection of two elements or the interaction between two elements.
  • the "first” or “under” of the second feature may include the first feature and the second feature in direct contact, or may include the first feature
  • the second feature is not in direct contact but is contacted by another feature between them.
  • the first feature is “above”, “above”, and “above” the second feature, including that the first feature is directly above and obliquely above the second feature, or merely indicates that the first feature is higher in level than the second feature.
  • the first feature is “below”, “below”, and “below” of the second feature, including the fact that the first feature is directly below and obliquely below the second feature, or merely indicates that the first feature is less horizontal than the second feature.
  • This embodiment provides a flue gas desulfurization, denitration, dust removal, and whitening device.
  • a flue gas inlet 1, a dust collector 2, a fan 3, and a stage 1 are sequentially connected through a flue gas pipe along the flue gas moving direction.
  • the flue gas produced by the factory is initially dusted by the dust collector 2 and sent to the first-stage absorption tower 6 through the fan 3.
  • the first-stage absorption tower 6 is desulfurized and denitrated by means of spraying agent absorption, and the spray layer of the first-stage absorption tower 6 There are multiple layers, and the spray agent is an alkaline agent, which can be removed by chemical reaction with sulfide and nitrate.
  • the spray agent is an alkaline agent, which can be removed by chemical reaction with sulfide and nitrate.
  • the flue gas after the two-stage desulfurization and denitration enters the pretreatment water washing tower 8 and is directly connected to the flue gas with circulating cooling water Air contact cooling, cooling the flue gas to below 45 degrees Celsius, reducing the water content in the saturated flue gas, circulating cooling water is circulated between the pretreatment water washing tower 8 and the cooling tower 11, and the cooling water is supplied to the flue gas in the pretreatment water washing tower 8 After the temperature is reduced to absorb heat, the heat is released in the cooling tower 11 to cool down, and then circulated to the pretreatment water washing tower 8 for recycling. After the flue gas has cooled down, it enters the wet electrostatic precipitator 9 to further remove the aerosol and moisture from the flue gas, and then is discharged through the flue gas outlet 12 on the top of the chimney 10.
  • the method further includes a first ozone dosing and spreading device 5 disposed between the fan 3 and the first-stage absorption tower 6, and a first ozone-feeding uniformizer 5 disposed between the first-stage absorption tower 6 and the second absorption tower 6.
  • the second ozone dosing and spreading device 13 between the stage absorption towers 7, the first ozone dosing and spreading device 5 and the second ozone dosing and spreading device 13 are connected to the ozone generator 4 through an ozone pipe.
  • the first-stage absorption tower 6 is provided with a first-stage absorption tower tray 601, a first-stage absorption tower spray layer 602, and a first-stage absorption tower demister 603 in this order along the moving direction of the flue gas.
  • the first-level absorption tower spray layer 602 is provided with three spray layers.
  • the secondary absorption tower 7 is sequentially provided with a secondary absorption tower tray 701, a secondary absorption tower spray layer 702, a secondary absorption tower packing layer 703, and a secondary absorption tower in the direction of flue gas movement.
  • the secondary absorption tower packing layer 703 is provided between the secondary absorption tower spraying layer 702 and the secondary absorption tower spraying layer 704, which can not only absorb the flat airflow, but also absorb sulfur oxides and nitrogen oxides, and more importantly, It is able to make the upper spraying layer 704 and the lower spraying layer 702 of the second absorption tower separately wash, and the slurry solubility between the two layers of washing is different, and it is more efficient to process the sulfur oxides in the flue gas. ,Nitrogen oxides.
  • the pretreatment water washing tower 8 is provided with a pretreatment water washing tower packing layer 801, a pretreatment water washing tower spray layer 802, and a pretreatment water washing tower demister 803 in this order along the flue gas moving direction.
  • the secondary absorption tower packing layer 703 is a ceramic packing
  • the pretreatment water washing tower packing layer 801 is a PP corrugated structured packing.
  • the first-stage absorption tower demister 603, the second-stage absorption tower demister 705, and the pretreatment water washing tower demister 803 are all folded plate demisters; as an optional implementation, the primary absorption tower tray 601 and the secondary absorption tower tray 701 are both alloy enhancement trays, and the alloy enhancement trays can improve airflow distribution.
  • the first spraying agent of the first-stage absorption tower 6 is a NaOH solution
  • the second spraying agent of the second-stage absorption tower 7 is a mixed solution of Na 2 SO 3 and NaHCO 3 .
  • the second spray agent is prepared by adding NaHCO 3 to the product absorbed by the first spray agent.
  • this application uses a gas-liquid direct heat exchange method to cool the flue gas.
  • the flue gas can be cooled by 6-12 ° C and discharged after removing water and mist by a wet electrostatic precipitator.
  • the design can achieve the design goals and effectively achieve the purpose of simultaneous desulfurization, denitrification and whitening.
  • This embodiment discloses a flue gas desulfurization, denitration, dust removal, and whitening device.
  • the differences from the first embodiment based on the embodiment are:
  • the first ozone dosing and spreading device and the second ozone dosing and spreading device are both ozone uniform distribution devices.
  • the ozone uniform distribution device in this embodiment includes a flue gas pipe 1 and a flue gas pipe is provided.
  • the ozone dosing device 2 in 1 is composed of a main inlet pipe 21 penetrating into the flue gas pipe 1 and a plurality of outlet nozzles 22 provided on the main inlet pipe 21.
  • the outlet nozzle 22 is along the main inlet pipe 21
  • the lengthwise intervals are uniformly arranged, and the connection between the main air inlet pipe 21 and the flue gas pipe 1 is sealed with a relevant sealant.
  • One end of the flue gas pipe 1 is a smoke inlet (not shown in the figure) and the other end is a smoke outlet (not shown in the figure).
  • the setting direction of the gas outlet nozzle 22 is consistent with the flow direction of the flue gas in the flue gas pipe 1.
  • the ozone-type uniform distribution device further includes a plurality of first units evenly spaced in the flue gas pipe 1.
  • the plurality of first units are arranged in parallel and vertically to each other.
  • the first unit and the outlet direction of the air outlet nozzle 22 Vertically, each outlet nozzle 22 includes two outlet gas heads 221 that communicate with the main intake pipe 21, and each outlet gas head 221 corresponds to a first unit.
  • the first unit is an oval tube 3. In this embodiment, the The distance between two adjacent oval tubes 3 is 100 mm.
  • the oval tube 3 is an elongated structure with an oval cross section.
  • the oval tube 3 is provided with a plurality of concave holes 31, and the plurality of concave holes 31 are evenly distributed along the length of the oval tube 3.
  • the distance between the air outlet nozzle 22 and the oval tube 3 is 300-400 mm.
  • the distance between the air outlet nozzle 22 and the bottom surface of the recess 31 is 360 mm.
  • an anticorrosive layer 32 is provided in the concave hole 31 on the oval tube 3.
  • the material of the anticorrosive layer 32 is PTFE (Poly TetraFluoroEthylene, polytetrafluoroethylene).
  • the anticorrosive layer 32 The material can also be EDPM (Ethylene-Propylene-Diene Monomer, ethylene propylene diene monomer), through the anti-corrosion layer 32 on the one hand can reduce the ozone gas on the oval tube 3 corrosion, on the other hand can slow the ozone gas flow on the oval tube 3 Shock.
  • a fixing plate 31 is provided on the top and bottom of the flue gas pipe 1, and the fixing plate 31 is fixedly connected to the oval pipe 3.
  • the two fixing plates 31 are arranged parallel to each other and flow with the flue gas in the flue gas pipe 1. The orientation is set vertically.
  • the oval ozone uniform distribution device further includes a plurality of second units fixed to the plurality of oval tubes 3.
  • the second unit is a strip-shaped structure, and the second unit may be channel steel or square steel.
  • It is a keel plate 4.
  • the keel plate 4 is 316L channel steel
  • the length of the oval tube 3 is 4300 mm
  • the length of the keel plate 4 is 7800 mm
  • the groove depth of the keel plate 4 is 50 mm and the width is 100 mm.
  • a plurality of keel plates 4 are evenly spaced along the length direction of the oval tube 3, and a plurality of keel plates 4 and a plurality of oval tubes 3 are vertically arranged.
  • one keel plate 4 is provided, and the keel plate 4 is provided. It is provided in the middle of the oval tube 3.
  • This embodiment discloses a flue gas desulfurization, denitration, dust removal, and whitening device.
  • the differences from the first embodiment based on the embodiment are:
  • the first ozone dosing and spreading device and the second ozone dosing and spreading device are both ozone equalizing devices.
  • the ozone equalizing device in this embodiment includes a flue gas pipe 1 and a flue gas pipe is provided.
  • the ozone dosing unit 2 in 1 includes the main intake pipe 21 penetrating into the flue gas pipe 1 and a plurality of outlet nozzles 22 uniformly arranged along the length of the main intake pipe 21.
  • the main intake pipe 21 The joint with the flue gas pipe 1 is sealed with relevant sealant.
  • One end of the flue gas pipe 1 is a smoke inlet (not shown in the figure) and the other end is a smoke outlet (not shown in the figure).
  • the setting direction of the gas outlet nozzle 22 is consistent with the flow direction of the flue gas in the flue gas pipe 1. .
  • the trough-type ozone uniform distribution device further includes a plurality of first trough plates 3 (as a first unit) which are evenly arranged in the flue gas pipe 1, and the plurality of first trough plates 3 are parallel to each other and vertical.
  • the distance between the outlet nozzle 22 and the bottom surface of the first slot plate 3 is 300-400mm.
  • the bottom surface of the slot 3 of the first slot plate is perpendicular to the outlet direction of the outlet nozzle 22.
  • Each outlet nozzle 22 includes 2 and
  • the main intake pipe 21 communicates with the exhaust gas head 221, and each exhaust gas head 221 corresponds to a first slotted plate 3.
  • the distance between two adjacent first slotted plates 3 is 100 mm
  • the outlet nozzle 22 to The distance between the bottom surfaces of the three grooves of the first groove plate is 360 mm.
  • a pair of long grooved plates 31 are disposed on the inner wall of the flue gas duct 1 in parallel.
  • One of the pair of long grooved plates 31 and one end of a plurality of first grooved plates 3 They are all fixedly connected, and the other long grooved plate 31 is fixedly connected to the other ends of the plurality of first grooved plates 3, and the long grooved plate 31 and the direction of the flow of the flue gas in the flue gas pipe 1 are vertically arranged.
  • the trough-type ozone uniform distribution device further includes a plurality of second trough plates 4 (as a second unit) which are fixed and communicated with the plurality of first trough plates 3.
  • the two grooved plates 4 are both elongated structures with a U-shaped cross section.
  • the first grooved plate 3 and the second grooved plate 4 are both 316L channel steel.
  • the length is 4300 mm
  • the length of the second grooved plate 4 is 7800 mm
  • the groove depth of the first grooved plate 3 and the second grooved plate 4 are both 50 mm
  • the width is 100 mm.
  • a plurality of second slotted plates 4 are arranged as a skeleton at regular intervals along the length direction of the first slotted plate 3.
  • a plurality of second slotted plates 4 and a plurality of first slotted plates 3 are vertically arranged.
  • one second grooved plate 4 is provided, and the second grooved plate 4 is provided in the middle of the first grooved plate 3.
  • Embodiment 4 is a diagrammatic representation of Embodiment 4:
  • this embodiment discloses a flue gas desulfurization, denitrification, dust removal, and whitening device, which is based on the third embodiment and is different from the third embodiment in that:
  • the angle between the symmetrical centerline of the first grooved plate 3 and the air outlet direction of the air outlet nozzle 22 is 30-60 °.
  • the intersection between the symmetrical centerline of the first grooved plate 3 and the air outlet direction of the air outlet nozzle 22 The angle is 30 °, and the two first grooved plates 3 provided corresponding to one outlet nozzle 22 are symmetrically disposed with respect to the center line of the outlet nozzle 22.

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Abstract

本申请属于烟气处理技术领域，公开了一种烟气脱硫脱硝除尘脱白装置，其沿烟气运动方向设置有通过烟气管道依次连接的烟气入口、除尘器、风机、一级吸收塔、二级吸收塔、预处理水洗塔、湿式电除尘器、烟筒和烟气出口，所述烟气出口设置在所述烟筒的顶部，所述水洗塔通过水管与冷却塔连接。

Description

一种烟气脱硫脱硝除尘脱白装置 技术领域
本申请涉及烟气处理技术领域，例如涉及一种烟气脱硫脱硝除尘脱白装置。
背景技术
燃料燃烧过程释放出的大量污染物(如SO 2、NO x、重金属、二噁英、VOCs、PM等)是环境日益恶化的主要原因，而燃烧后烟气的净化是控制污染排放的有效途径之一。针对烟气脱硫脱硝，目前国内外燃煤电厂广泛使用NH 3选择性催还原(NH 3-SCR)脱硝和湿法烟气脱硫(WFGD)的技术组合。该技术组合虽具有较高的脱硫脱硝效率，但不适用于钢铁烧结和部分工业锅炉等炉窑烟气的处理，其原因是此类烟气温度较低而且波动范围大，污染物浓度波动幅度大且成分复杂，易造成催化剂中毒。并且，单独脱硫脱硝技术往往会引起系统庞杂、占地面积大、投资运行费用高等问题。继火电行业全面实施超低排放改造之后，各类工业炉窑将成为我国最主要的大气污染排放源。
脱硫脱硝后烟气为饱和烟气和微量的气溶胶等污染物，看上去排出的是“白烟”，为了比较彻底去除烟气中有害成分，包括减少氮氧化物、硫化物、各种烟尘颗粒物、气溶胶、超细结晶盐颗粒物的排放，减少烟囱雨的发生和满足人们的视觉美观，在脱硫脱硝后还需要“烟气脱白”，但相关的烟气脱白方法，系统结构复杂，需要在抬升温度较大，能耗高，不利于节能减排。湿法脱硫脱硝脱白，不仅能根除雾霾污染，还能低成本实现环保达标、超低近零排放，年节水潜力几十亿吨，能兼顾解决环境与发展的矛盾。
CN107983078A公开了一种脱白零排放系统，将冷却水冷却和静电捕捉液滴的功能合成一个整体，以解决湿法脱硫工艺进行脱硫处理时产生的白色烟带问 题。其冷却是用冷却水管热交换的方式实现，使用电场用静电捕捉液滴，耗电量较大，且整体结构较复杂，适宜处理烟气的量较小。CN107781832A公开了一种燃煤湿法脱硫烟气脱水再热余热利用排放系统，通过设置烟气显热回收循环和烟气潜热回收循环，以实现烟气中余热的回收和利用，对脱硫处理后的烟气进行喷淋降温脱水处理，回收烟气释放的潜热；喷淋降温脱水处理后的烟气经过烟气加热器的加热处理后排放至大气。而喷淋降温后再加热后排放，可能在此喷淋过程中增加烟气中湿度，降低脱白的效果。
综上所述，相关技术仍缺少一种适用范围广、脱硫脱硝脱白一体化、可同步去除多种污染物的烟气净化技术。
发明内容
以下是对本文详细描述的主题的概述。本概述并非是为了限制权利要求的保护范围。
本申请的目的在于提供一种烟气脱硫脱硝除尘脱白装置，适用范围广、脱硫脱硝脱白一体化、可同步去除多种污染物，并且装置成本低、能够持续稳定运行。
为达此目的，本申请采用以下技术方案：
一种烟气脱硫脱硝除尘脱白装置，沿烟气运动方向设置有通过烟气管道依次连接的除尘器、风机、一级吸收塔、二级吸收塔、预处理水洗塔、湿式电除尘器、烟筒，所述除尘器设置有烟气入口，所述烟筒的顶部设置有烟气出口，所述水洗塔通过水管与冷却塔连接。
工厂产生的烟气经过除尘器初步除尘后，通过风机送入一级吸收塔，一级吸收塔用喷淋药剂来吸收的方式进行脱硫脱硝，一级吸收塔的喷淋层有多层，喷淋药剂为碱性试剂，可以与硫化物和硝化物发生化学反应而被除去。烟气在 进行了第一级吸收后，然后进入二级吸收塔喷淋吸收以进行深度脱硫脱硝，进行过两级脱硫脱硝后的烟气进入预处理水洗塔用循环冷却水直接与烟气接触降温，将烟气冷却到45摄氏度以下，降低饱和烟气中的含水量，循环冷却水在预处理水洗塔和冷却塔之间循环，冷却水在预处理水洗塔给烟气降温吸收热量后，在冷却塔中放出热量降温，然后循环至预处理水洗塔中循环使用。烟气降温后，进入湿式电除尘器进一步除去气溶胶和烟气中水分，然后通过烟囱顶部的烟气出口排出。
本申请的第一个核心是通过水冷进一步降低烟气温度。烟气颜色容易变成白色，是因为烟气出口排出的烟气温度约为60℃左右，相比室外环境的温度10-30℃要高很多，此时高温烟气与大气混合后，温度降低幅度较大，当温度降至露点温度以下时，水蒸气就会结露，烟气中残留的硫化物就会与水发生反应生成亚硫酸，亚硫酸不稳定，容易被氧化生成硫酸小液滴，也就是“白烟”。本申请通过冷却塔输入冷却水，使得烟气在水洗塔内冷却水循环洗涤，用循环冷却水直接与烟气接触降温，可以将烟气冷却到45摄氏度以下。出口烟气的温度降低了10-15摄氏度，能够大幅减少“白烟”，实践中证明，可以使得“白烟”减少60-90％以上。
作为可选的技术方案，还包括设置于所述风机和所述一级吸收塔之间的第一臭氧投加均布器，以及设置于所述一级吸收塔与所述二级吸收塔之间的第二臭氧投加均布器，所述第一臭氧投加均布器和所述第二臭氧投加均布器与臭氧发生器通过臭氧管道连接。
本申请的第二个核心是在烟道中投加臭氧，所述一级吸收塔与所述二级吸收塔均采用臭氧氧化结合湿法洗涤的技术路线，利用强氧化性臭氧O 3将烟气中的硫氧化物、氮氧化物氧化成易被吸收的高价硫氧化物、氮氧化物。烟气中所 含硫氧化物SO x及氮氧化物NO x与臭氧起氧化反应，具体反应式如下：
SO 2+O 3→SO 3+O 2  NO+O 3→NO 2+O 2   2NO 2+O 3→O 2+N 2O 5
经过上述臭氧处理步骤后，烟气进入了洗涤塔，本申请是在采用臭氧氧化结合湿法洗涤的技术路线，利用强氧化性O 3将烟气中难溶于水的NO氧化成水溶性较好的高价态氮氧化物(如NO 2、NO 3、N 2O 5等)，进而实现SO 2和NO x的一体化脱除。
作为可选的技术方案，所述一级吸收塔沿烟气运动方向依次设置有一级吸收塔托盘、一级吸收塔喷淋层、一级吸收塔除雾器。所述一级吸收塔喷淋层设置有3层喷淋。一级吸收塔可以对硫氧化物、氮氧化物进行初步处理。
作为可选的技术方案，所述二级吸收塔沿烟气运动方向依次设置有二级吸收塔托盘、二级吸收塔下喷淋层、二级吸收塔填料层、二级吸收塔上喷淋层、二级吸收塔除雾器。所述二级吸收塔填料层设置有二级吸收塔下喷淋层和二级吸收塔上喷淋层之间，不仅能够吸收平整气流和吸收硫氧化物、氮氧化物，更重要的是能够使得二级吸收塔上喷淋层和二级吸收塔下喷淋层分别洗涤，而且两层洗涤之间的浆液溶度是有差异的，更能够高效处理烟气中的硫氧化物、氮氧化物。二级吸收塔下喷淋层和二级吸收塔上喷淋层均为两层喷淋。增加了二级吸收塔，相比以往的一级吸收，能够深度处理烟气中的硫氧化物、氮氧化物，脱硫脱硝效果更佳。
作为可选的技术方案，预处理水洗塔沿烟气运动方向依次设置有预处理水洗塔填料层、预处理水洗塔喷淋层、预处理水洗塔除雾器。预处理水洗塔主要是为了给烟气降温，预处理水洗塔喷淋剂来自与冷却塔的循环冷却水，成本低，处理效果好，而且能够持续稳定运行。
作为可选的技术方案，所述二级吸收塔填料层为陶瓷填料，所述预处理水 洗塔填料层为PP(聚丙烯)波纹规整填料。
作为可选的技术方案，所述一级吸收塔除雾器、二级吸收塔除雾器和所述预处理水洗塔除雾器均为折板除雾器；作为可选的实施例，所述一级吸收塔托盘和二级吸收塔托盘均为合金增效托盘，所述合金增效托盘可以改进气流分布。
作为可选的技术方案，所述一级吸收塔的第一喷淋药剂为NaOH溶液，所述二级吸收塔所使用的第二喷淋药剂Na 2SO 3和NaHCO 3混合溶液。
本申请的第三个核心是烟气经过两级循环洗涤，而且一级吸收塔和二级吸收塔所使用的喷淋药剂是不同的。采用NaOH溶液进行同时脱硫脱硝时，SO 2与NaOH溶液之间的反应是优先进行的，SO 2能够与NaOH迅速反应并生成SO 3 2-离子，具有很高的脱除效率；但高浓度SO 2对NO x在NaOH溶液中的吸收存在一定的抑制作用，且NO x与NaOH间的反应本就存在反应速率低、脱除效率不理想等问题，因此烟气中SO 2能够实现达标，但NO x达标情况难以保证。由于Na 2SO 3和NaHCO 3较NaOH对NO x表现出更佳的还原效果，因此通过此分区、分侧重点的一塔脱硫脱硝工艺，能够实现较高的脱硫脱硝效率。可选地，所述第一喷淋药剂为NaOH溶液脱硫产物为Na 2SO 3。
作为可选的技术方案，所述第二喷淋药剂为第一喷淋药剂吸收后的产物加入NaHCO 3配制而成。可以选用第一喷淋药剂脱硫产物为Na 2SO 3，加入NaHCO 3作为缓冲剂，配制成所述第二喷淋药剂，能够循环使用，节约资源。臭氧氧化结合两级湿法洗涤，能够实现脱硫脱硝更加地彻底。
作为可选的技术方案，所述预处理水洗塔的冷却水流量Q 水与所述烟气流量Q 气满足关系式：Q水＝β×(t 1-t 2)×Q 气，β为冷却比例系数，t 1为烟气入口的烟气温度，t 2为烟气出口的烟气温度，β的值位于200-300之间。
设定入口烟气流量Q 气，密度ρ 1，温度t 1，比热容C 1；出口烟气流量不变为 Q 气，密度ρ 2，温度t 2，比热容C 2。冷却水流量Q 水，密度ρ 水，入口温度T 1，比热容C 水1，出口温度T 2，出口比热容C 水2，h是处理时间。
则：
ρ 1×Q 气×h×t 1+Q 水×h×C 水1×T 1＝ρ 2×Q 气×h×t 2+ρ 水×Q 水×h×C 水2×T 2
然而，化工的实际生产过程是复杂的，如放大效应等，会带来较大的损耗，且水量小也可能达不到喷淋覆盖的要求，因此，取一个工况参数κ，放大一定的倍数，确保所需的水量足够，进而得出Q 水＝κ×λ×Q 气。κ≥2,同时，循环冷却水的入口温度和出口温度在通常的工况下较为稳定，通常可以认为T 2与T 1的差值为5-8之间，所以，可以得出Q 水＝β×(t 1-t 2)×Q 气，β的值位于200-300之间。
作为可选的技术方案，所述第一臭氧投加均布器和所述第二臭氧投加均布器均为臭氧均布装置，所述臭氧均布装置包括烟气管道以及设置于烟气管道内的臭氧投加器，臭氧投加器包括一主进气管以及若干设置于主进气管的出气喷头，所述臭氧均布装置还包括设置于烟气管道内的若干第一单元以及若干第二单元，若干第一单元相互平行且间隔设置，若干第二单元与若干第一单元固定连接，所述出气喷头的出气口朝第一单元设置。
作为可选的技术方案，所述第一单元为椭圆管，所述第二单元为龙骨板。
作为可选的技术方案，所述椭圆管上沿其长度方向均布有若干凹孔，所述凹孔正对于出气喷头设置。
作为可选的技术方案，所述凹孔内设置有防腐层。
作为可选的技术方案，所述第一单元为第一槽形板，所述第二单元为第二槽形板，若干第二槽型板与若干第一槽型板均连通，第一槽型板与第二槽型板的开口均朝出气喷头的出气口设置。
作为可选的技术方案，所述第一槽型板的开口正对于出气喷头的出气口。
作为可选的技术方案，所述第一槽型板的对称中心线与出气喷头的出气方向成30～60°的夹角。
本申请的有益效果包括：
1、整合了臭氧氧化、化学药剂吸收脱硫脱硝、喷淋冷却降温和电除尘器除湿的技术，用一个简洁完整的工艺流程实现烟气脱硫脱硝脱白，能高效去除烟气中的烟尘、氮氧化物和二氧化硫，有效去除尾气中水分，脱除白烟。设备维护简单，能源消耗低。
2、两级循环洗涤，而且一级吸收塔和二级吸收塔所使用的喷淋药剂是不同的，可以达到更合适的脱硫脱硝。
3、装置设计合理，工艺过程、设备结构紧凑，装置成本低、能够持续稳定运行，提高烟气净化的经济性。
在阅读并理解了详细描述和附图后，可以明白其他方面。
附图说明
图1为本申请实施例中装置的工艺流程示意图；
图2为本申请实施例一中椭圆管与龙骨板的布置示意图；
图3是本申请实施例一中椭圆管与臭氧投加器的布置示意图；
图4为图3中A部的放大图；
图5是本申请实施例二中第一槽型板与臭氧投加器的布置示意图；
图6为本申请实施例二中第一槽型板与第二槽型板的布置示意图；
图7为图6中A-A面的剖视图；
图8为本申请实施例三中第一槽型板与臭氧投加器的布置示意图。
图1中，各附图标记所指代的技术特征如下：1、烟气入口；2、除尘器；3、 风机；4、臭氧发生器；5、第一臭氧投加均布器；6、一级吸收塔；601、一级吸收塔托盘；602、一级吸收塔喷淋层；603、一级吸收塔除雾器；7、二级吸收塔；701、二级吸收塔托盘；702、二级吸收塔下喷淋层；703、二级吸收塔填料层；704、二级吸收塔上喷淋层；705、二级吸收塔除雾器；8、预处理水洗塔；801、预处理水洗塔填料层；802、预处理水洗塔喷淋层；803、预处理水洗塔除雾器；9、湿式电除尘器；10、烟筒；11、冷却塔；12、烟气出口；13、第二臭氧投加均布器。
图2-图4中，各附图标记所指代的技术特征如下：1、烟气管道；2、臭氧投加器；21、主进气管；22、出气喷头；221、支出气头；3、椭圆管；31、凹孔；32、防腐层；31、固定板；4、龙骨板。
图5-图8中，各附图标记所指代的技术特征如下：1、烟气管道；2、臭氧投加器；21、主进气管；22、出气喷头；221、支出气头；3、第一槽型板；31、长槽型板；4、第二槽型板。
具体实施方式
下面详细描述本申请的实施例，实施例的示例在附图中示出，其中自始至终相同或类似的标号表示相同或类似的元件或具有相同或类似功能的元件。下面通过参考附图描述的实施例是示例性的，旨在用于解释本申请，而不能理解为对本申请的限制。
在本申请的描述中，除非另有明确的规定和限定，术语“相连”、“连接”、“固定”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，可以是机械连接，也可以是电连接，可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通或两个元件的相互作用关系。对于本领域的普通技术人员而言，可以根据具体情况理解上述术语在本申请中的具体含义。
在本申请的描述中，除非另有明确的规定和限定，第一特征在第二特征之“上”或之“下”可以包括第一特征和第二特征直接接触，也可以包括第一特征和第二特征不是直接接触而是通过它们之间的另外的特征接触。而且，第一特征在第二特征“之上”、“上方”和“上面”包括第一特征在第二特征正上方和斜上方，或仅仅表示第一特征水平高度高于第二特征。第一特征在第二特征“之下”、“下方”和“下面”包括第一特征在第二特征正下方和斜下方，或仅仅表示第一特征水平高度小于第二特征。
下面结合附图并通过具体实施方式来进一步说明本申请的技术方案。
实施例一：
本实施例提供了一种烟气脱硫脱硝除尘脱白装置，如图1所示，沿烟气运动方向设置有通过烟气管道依次连接的烟气入口1、除尘器2、风机3、一级吸收塔6、二级吸收塔7、预处理水洗塔8、湿式电除尘器9、烟筒10和烟气出口12，所述烟气出口12设置在所述烟筒10的顶部，所述水洗塔8通过水管与冷却塔11连接。
工厂产生的烟气经过除尘器2初步除尘后，通过风机3送入一级吸收塔6，一级吸收塔6用喷淋药剂来吸收的方式进行脱硫脱硝，一级吸收塔6的喷淋层有多层，喷淋药剂为碱性试剂，可以与硫化物和硝化物发生化学反应而被除去。烟气在进行了第一级吸收后，然后进入二级吸收塔7喷淋吸收以进行深度脱硫脱硝，进行过两级脱硫脱硝后的烟气进入预处理水洗塔8用循环冷却水直接与烟气接触降温，将烟气冷却到45摄氏度以下，降低饱和烟气中的含水量，循环冷却水在预处理水洗塔8和冷却塔11之间循环，冷却水在预处理水洗塔8给烟气降温吸收热量后，在冷却塔11中放出热量降温，然后循环至预处理水洗塔8中循环使用。烟气降温后，进入湿式电除尘器9进一步除去气溶胶和烟气中水 分，然后通过烟囱10顶部的烟气出口12排出。
作为可选的实施例，还包括设置于所述风机3和所述一级吸收塔6之间的第一臭氧投加均布器5，以及设置于所述一级吸收塔6与所述二级吸收塔7之间的第二臭氧投加均布器13，所述第一臭氧投加均布器5和所述第二臭氧投加均布器13与臭氧发生器4通过臭氧管道连接。
作为可选的实施例，所述一级吸收塔6沿烟气运动方向依次设置有一级吸收塔托盘601、一级吸收塔喷淋层602、一级吸收塔除雾器603。所述一级吸收塔喷淋层602设置有3层喷淋。
作为可选的实施例，所述二级吸收塔7沿烟气运动方向依次设置有二级吸收塔托盘701、二级吸收塔下喷淋层702、二级吸收塔填料层703、二级吸收塔上喷淋层704、二级吸收塔除雾器705。所述二级吸收塔填料层703设置有二级吸收塔下喷淋层702和二级吸收塔上喷淋层704之间，不仅能够吸收平整气流和吸收硫氧化物、氮氧化物，更重要的是能够使得二级吸收塔上喷淋层704和二级吸收塔下喷淋层702分别洗涤，而且两层洗涤之间的浆液溶度是有差异的，更能够高效处理烟气中的硫氧化物、氮氧化物。
作为可选的实施例，预处理水洗塔8沿烟气运动方向依次设置有预处理水洗塔填料层801、预处理水洗塔喷淋层802、预处理水洗塔除雾器803。
作为可选的实施例，所述二级吸收塔填料层703为陶瓷填料，所述预处理水洗塔填料层801为PP波纹规整填料。
作为可选的实施例，所述一级吸收塔除雾器603、二级吸收塔除雾器705和所述预处理水洗塔除雾器803均为折板除雾器；作为可选的实施例，所述一级吸收塔托盘601和二级吸收塔托盘701均为合金增效托盘，所述合金增效托盘可以改进气流分布。
作为可选的实施例，所述一级吸收塔6的第一喷淋药剂为NaOH溶液，所述二级吸收塔7所使用的第二喷淋药剂Na 2SO 3和NaHCO 3混合溶液。所述第二喷淋药剂为第一喷淋药剂吸收后的产物加入NaHCO 3配制而成。
作为可选的实施例，所述预处理水洗塔8的冷却水流量Q 水与所述烟气流量Q 气满足关系式：Q 水＝β×(t 1-t 2)×Q 气，β为冷却比例系数，t 1为烟气入口的烟气温度，t 2为烟气出口的烟气温度，β的值位于200-300之间。
应用实施例
将本装置应用于唐山燕山钢铁有限公司300m 2烧结烟气脱硝及脱硫除尘治理项目，在现有正常稳定运行烟气量条件下，测定入口烟气流量Q 气＝1368700m 3/h，密度ρ 1＝1.043Kg/m 3，温度t 1＝50℃，比热容C 1＝1.056Kj/(Kg℃)；出口烟气流量不变为Q 气，密度ρ 2＝1.091Kg/m 3，温度t 2＝43℃，比热容C 2＝1.055Kj/(Kg℃)。冷却水密度ρ 水＝1000Kg/m 3，入口温度T 1＝25℃，比热容C 水 1＝4.1846Kj/(Kg℃)，出口水的温度T 2＝30℃，出口比热容C 水2＝4.1807Kj/(Kg℃)，h是处理时间，则降温脱白所需的最小水量Q 水＝κ×λ×Q 气＝728.96m 3/h，比较合适的β的值为268。在实际的工况运行中，得到下列测试结果。
Figure PCTCN2019090487-appb-000001
Figure PCTCN2019090487-appb-000002
由项目1、6、11可知，当β值过小时，需要较多的冷却水才能够得到温度降低，由5、10、15可知，当β值过大时，冷却水较小，达不到足够冷却的效果。因此，根据长期的工况调整中,得到如下的试验结果:Q 水＝β×(t 1-t 2)×Q 气,是经过一系列工程实践得出的最合适的比例，既可以节约冷却水用量，又能够保证气体温度的降低。所述臭氧发生器4投加的臭氧投加量Y在合适的范围的内，能够较好地氧化烟气中的低价氧化物。综上，本申请采用气液直接换热的方式冷却烟气，替代热交换器，可将烟气降温6-12℃，通过湿式电除尘器除水除雾后排放。该设计可达到设计目标，有效实现同步脱硫脱硝脱白的目的。
实施例二：
本实施例公开了一种烟气脱硫脱硝除尘脱白装置，基于实施例一并与实施例一区别的地方在于：
第一臭氧投加均布器和第二臭氧投加均布器均为臭氧均布装置，参考图2以及图3，本实施例中的臭氧均布装置包括烟气管道1以及设置烟气管道1内的 臭氧投加器2，臭氧投加器2包括穿设进烟气管道1中的主进气管21以及若干设置于主进气管21上的出气喷头22，出气喷头22沿主进气管21的长度方向间隔均匀设置，主进气管21与烟气管道1的连接处采用相关的密封胶做密封处理。
烟气管道1一端为进烟口(图中未示出)，另一端为出烟口(图中未示出)，出气喷头22的设置方向与烟气管道1内烟气的流动方向一致。
参考图2以及图3，型臭氧均布装置还包括若干间隔均匀设置于烟气管道1内的第一单元，若干第一单元相互平行且竖直设置，第一单元与出气喷头22的出气方向垂直，每一出气喷头22包括2个与主进气管21连通支出气头221，每一支出气头221对应一第一单元，具体地，第一单元为椭圆管3，本实施例中，相邻的2个椭圆管3的间距为100mm。
参考图2以及图3，椭圆管3为截面为椭圆形的长条状结构，椭圆管3上设置有若干凹孔31，若干凹孔31沿椭圆管3的长度方向均匀分布，凹孔31正对于支出气头221的出气口，出气喷头22到椭圆管3的距离为300～400mm，本实施例中，出气喷头22到凹孔31底面的距离为360mm。
参考图3以及图4，椭圆管3上位于凹孔31内设置有防腐层32，防腐层32的材料为PTFE(Poly Tetra Fluoro Ethylene，聚四氟乙烯)，在其他实施例中，防腐层32的材料还可以为EDPM(Ethylene-Propylene-Diene Monomer，乙烯丙烯二烯单体)，通过防腐层32一方面可减少臭氧气流对椭圆管3的腐蚀，另一方面可减缓臭氧气流对椭圆管3的冲击。
参考图2以及图3，烟气管道1的顶部与底部均设置有固定板31，固定板31均与椭圆管3固定连接，两固定板31相互平行设置且与烟气管道1内烟气流动的方向垂直设置。
参考图2以及图3，椭圆型臭氧均布装置还包括与若干椭圆管3均固定的若 干第二单元，第二单元为长条形状结构，第二单元可为槽钢或方钢，具体地为龙骨板4，本实施例中，龙骨板4为316L槽钢，椭圆管3的长度为4300mm，龙骨板4的长度为7800mm，龙骨板4的槽深度为50mm、宽度为100mm。
参考图2以及图3，若干龙骨板4沿椭圆管3的长度方向间隔均匀设置，若干龙骨板4与若干椭圆管3均垂直设置，本实施例中，龙骨板4设置一个，该龙骨板4设置于椭圆管3的中部。
实施例三：
本实施例公开了一种烟气脱硫脱硝除尘脱白装置，基于实施例一并与实施例一区别的地方在于：
第一臭氧投加均布器和第二臭氧投加均布器均为臭氧均布装置，参考图5以及图6，本实施例中的臭氧均布装置包括烟气管道1以及设置烟气管道1内的臭氧投加器2，臭氧投加器2包括穿设进烟气管道1中的主进气管21以及沿主进气管21的长度方向间隔均匀设置的若干出气喷头22，主进气管21与烟气管道1的连接处采用相关的密封胶做密封处理。
烟气管道1的一端为进烟口(图中未示出)，另一端为出烟口(图中未示出)，出气喷头22的设置方向与烟气管道1内烟气的流动方向一致。
参考图5以及图6，槽型臭氧均布装置还包括若干间隔均匀设置于烟气管道1内的第一槽型板3(作为第一单元)，若干第一槽型板3相互平行且竖直设置，出气喷头22到第一槽型板3槽底面的距离为300～400mm，第一槽型板3槽的底面与出气喷头22的出气方向垂直，每一出气喷头22均包括2个与主进气管21连通支出气头221，每一支出气头221对应一第一槽型板3，本实施例中，相邻的2个第一槽型板3的间距为100mm，出气喷头22到第一槽型板3槽底面的距离为360mm。
参考图6以及图7，烟气管道1内壁上设置有平行设置的一对长槽型板31，一对长槽型板31其中一长槽型板31与若干第一槽型板3的一端均固定连接，另一长槽形板31与若干第一槽型板3的另一端均固定连接，长槽型板31与烟气管道1内烟气流动的方向垂直设置。
参考图6以及图7，槽型臭氧均布装置还包括与若干第一槽型板3均固定并连通的若干第二槽型板4(作为第二单元)，第一槽型板3与第二槽型板4均为截面为“U”形的长条形状结构，本实施例中，第一槽型板3与第二槽型板4均为316L槽钢，第一槽型板3的长度为4300mm，第二槽型板4的长度为7800mm，第一槽型板3与第二槽型板4的槽深度均为50mm、宽度均为100mm。
参考图6以及图7，若干第二槽型板4作为骨架沿第一槽型板3的长度方向间隔均匀设置，若干第二槽型板4与若干第一槽型板3均垂直设置，本实施例中，第二槽型板4设置一个，该第二槽型板4设置于第一槽型板3的中部。
实施例四：
参考图8，本实施例公开了一种烟气脱硫脱硝除尘脱白装置，基于实施例三并与实施例三区别的地方在于：
第一槽型板3的对称中心线与出气喷头22的出气方向成30～60°的夹角，本实施例中，第一槽型板3的对称中心线与出气喷头22的出气方向的夹角为30°，对应一个出气喷头22设置的2个第一槽型板3关于出气喷头22的中心线对称设置。
显然，本申请的上述实施例仅仅是为了清楚说明本申请所作的举例，而并非是对本申请的实施方式的限定。对于所属领域的普通技术人员来说，在上述说明的基础上还可以做出其它不同形式的变化或变动。这里无需也无法对所有的实施方式予以穷举。

Claims (17)

  1. 一种烟气脱硫脱硝除尘脱白装置，其中，沿烟气运动方向设置有通过烟气管道依次连接的除尘器、风机、一级吸收塔、二级吸收塔、预处理水洗塔、湿式电除尘器、烟筒，所述除尘器设置有烟气入口，所述烟筒在顶部设置有烟气出口，所述预处理水洗塔通过水管与冷却塔连接。
  2. 根据权利要求1所述的烟气脱硫脱硝除尘脱白装置，其中，还包括设置于所述风机和所述一级吸收塔之间的第一臭氧投加均布器，以及设置于所述一级吸收塔与所述二级吸收塔之间的第二臭氧投加均布器，所述第一臭氧投加均布器和所述第二臭氧投加均布器与臭氧发生器通过臭氧管道连接。
  3. 根据权利要求1或2所述的烟气脱硫脱硝除尘脱白装置，其中，所述一级吸收塔使用的第一喷淋药剂为NaOH溶液，所述二级吸收塔使用的第二喷淋药剂为Na 2SO 3和NaHCO 3混合溶液。
  4. 根据权利要求2所述的烟气脱硫脱硝除尘脱白装置，其中，所述一级吸收塔沿烟气运动方向设置有一级吸收塔托盘、一级吸收塔喷淋层、一级吸收塔除雾器。
  5. 根据权利要求2所述的烟气脱硫脱硝除尘脱白装置，其中，所述二级吸收塔沿烟气运动方向依次设置有二级吸收塔托盘、二级吸收塔下喷淋层、二级吸收塔填料层、二级吸收塔上喷淋层、二级吸收塔除雾器。
  6. 根据权利要求2所述的烟气脱硫脱硝除尘脱白装置，其中，所述预处理水洗塔沿烟气运动方向依次设置有预处理水洗塔填料层、预处理水洗塔喷淋层、预处理水洗塔除雾器。
  7. 根据权利要求4或5或6所述的烟气脱硫脱硝除尘脱白装置，其中，所述二级吸收塔填料层为陶瓷填料，所述预处理水洗塔填料层为PP波纹规整填料。
  8. 根据权利要求4或5或6所述的烟气脱硫脱硝除尘脱白装置，其中，所述一级吸收塔除雾器、二级吸收塔除雾器和所述预处理水洗塔除雾器均为折板除雾器；所述一级吸收塔托盘和二级吸收塔托盘均为合金增效托盘，所述合金增效托盘可以改进气流分布。
  9. 根据权利要求3所述的烟气脱硫脱硝除尘脱白装置，其中，所述第二喷淋药剂为第一喷淋药剂吸收后的产物加入NaHCO 3配制而成。
  10. 根据权利要求1所述的烟气脱硫脱硝除尘脱白装置，其中，所述预处理水洗塔的冷却水流量Q 水与所述烟气流量Q 气满足关系式：Q 水＝β×(t 1-t 2)×Q 气，β为冷却比例系数，t 1为烟气入口的烟气温度，t 2为烟气出口的烟气温度，β的值位于200-300之间。
  11. 根据权利要求2所述的烟气脱硫脱硝除尘脱白装置，其中，所述第一臭氧投加均布器和所述第二臭氧投加均布器均为臭氧均布装置，所述臭氧均布装置包括烟气管道以及设置于烟气管道内的臭氧投加器，臭氧投加器包括一主进气管以及若干设置于主进气管的出气喷头，所述臭氧均布装置还包括设置于烟气管道内的若干第一单元以及若干第二单元，若干第一单元相互平行且间隔设置，若干第二单元与若干第一单元固定连接，所述出气喷头的出气口朝第一单元设置。
  12. 根据权利要求11所述的烟气脱硫脱硝除尘脱白装置，其中，所述第一单元为椭圆管，所述第二单元为龙骨板。
  13. 根据权利要求12所述的烟气脱硫脱硝除尘脱白装置，其中，所述椭圆管上沿其长度方向均布有若干凹孔，所述凹孔正对于出气喷头设置。
  14. 根据权利要求13所述的烟气脱硫脱硝除尘脱白装置，其中，所述凹孔内设置有防腐层。
  15. 根据权利要求11所述的烟气脱硫脱硝除尘脱白装置，其中，所述第一单元为第一槽形板，所述第二单元为第二槽形板，若干第二槽型板与若干第一槽型板均连通，第一槽型板与第二槽型板的开口均朝出气喷头的出气口设置。
  16. 根据权利要求15所述的烟气脱硫脱硝除尘脱白装置，其中，所述第一槽型板的开口正对于出气喷头的出气口。
  17. 根据权利要求15所述的烟气脱硫脱硝除尘脱白装置，其中，所述第一槽型板的对称中心线与出气喷头的出气方向成30～60°的夹角。
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