CN108786398A - Flue gas desulfurization regenerates integrated tower and Regeneratable wet fuel gas desulfurizing method - Google Patents

Flue gas desulfurization regenerates integrated tower and Regeneratable wet fuel gas desulfurizing method Download PDF

Info

Publication number
CN108786398A
CN108786398A CN201710299537.6A CN201710299537A CN108786398A CN 108786398 A CN108786398 A CN 108786398A CN 201710299537 A CN201710299537 A CN 201710299537A CN 108786398 A CN108786398 A CN 108786398A
Authority
CN
China
Prior art keywords
zone
flue gas
liquid
partition board
tower
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201710299537.6A
Other languages
Chinese (zh)
Other versions
CN108786398B (en
Inventor
何佳
李欣
李磊
王晶
王昊辰
韩天竹
金平
王海波
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
Original Assignee
China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Dalian Research Institute of Petroleum and Petrochemicals filed Critical China Petroleum and Chemical Corp
Priority to CN201710299537.6A priority Critical patent/CN108786398B/en
Publication of CN108786398A publication Critical patent/CN108786398A/en
Application granted granted Critical
Publication of CN108786398B publication Critical patent/CN108786398B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
    • B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
    • 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
    • B01D53/343—Heat recovery
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/12—Methods and means for introducing reactants
    • B01D2259/124—Liquid reactants

Landscapes

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

Abstract

The invention discloses flue gas desulfurization regeneration integrated tower and Regeneratable wet fuel gas desulfurizing methods.Flue gas desulfurization regenerates integrated tower, is from top to bottom followed successively by flue gas emission area, mist eliminating zone, two level spraying zone, holds liquid bath area, level-one spraying zone and regeneration of absorption solution area；Regeneration of absorption solution area is from left to right divided into preheating zone, stripping zone and liquid collecting zone successively by vertical clapboard I, partition board II and partition board III, preheating zone is connected to level-one spraying zone, partition board I bottom openings make preheating zone be connected to stripping zone, the height of partition board II is less than the height of partition board I, stripping zone is connected to liquid collecting zone by the space on the tops partition board II, by partition board III that stripping zone and liquid collecting zone and spraying zone is completely separated at the top of stripping zone and liquid collecting zone；Set of heat exchange tubes is arranged in preheating zone, and flue gas is entered by set of heat exchange tubes in tower；Outer sleeve is arranged in the chimney top in flue gas emission area.The present invention realizes SO in flue gas2Recycling and depth demisting, technological process is short, equipment is few, operating cost is low, has broad application prospects.

Description

Flue gas desulfurization regenerates integrated tower and Regeneratable wet fuel gas desulfurizing method
Technical field
The invention belongs to industrial waste gas purifying field, it is related to a kind of flue gas desulfurization regeneration integrated tower and Regeneratable wet flue gas Sulfur method.
Background technology
It is well known that sulfur dioxide is one of major pollutants of air, even more cause " arch-criminal " of acid rain.According to What Ministry of Environmental Protection announced《Environment bulletin in 2015》, 480, China city（Area, county）Rainfall Monitoring the result shows that：Acid Rain frequency averaging is 14.0%, and the city ratio for acid rain occur is 40.4%, and acid rain frequency is in 25% or more city ratio 20.8%, acid rain frequency is 12.7% in 50% or more city ratio, and acid rain frequency is 5.0% in 75% or more city ratio；Drop Anion in water is sulfate radical, accounts for the 24.7% of total ion concentration, and acid rain type type of population is still sulfuric acid type.
Environmental pollution getting worse, haze event take place frequently, and country is also higher and higher to the attention degree of environmental protection, goes out in recent years A series of platform laws and regulations, national standard and the management method of environmental protections.GB13271-2014《Boiler atmosphere pollution is arranged Put standard》Regulation：Newly-built coal-burning boiler, oil burning boiler, gas fired-boiler discharge flue gas SO2Concentration limit is respectively 300,200, 50mg/Nm3, coal-burning boiler, oil burning boiler, the gas fired-boiler discharge flue gas SO of key area2Concentration limit is respectively 200,100, 50mg/Nm3.GB 13223-2011 《Fossil-fuel power plant atmospheric pollutant emission standard》Regulation：The SO of new construction of coal-fired boiler flue gas2≯ 100mg/Nm3, key area coal-burning boiler SO2≯50mg/Nm3.《Implement in full coal-burning power plant's minimum discharge and reducing energy consumption work Make scheme》（Ring sends out [2015] No. 164）Middle regulation coal-fired plant flue gas minimum discharge index is： SO2≯35mg/Nm3。GB 31570-2015《Petroleum refining industry pollutant emission standard》Regulation：Catalytic cracking catalyst regenerated flue gas, SO2≯100mg/ Nm3, key area SO2≯50mg/Nm3。
The purification techniques of SO 2 from fume is divided into three kinds of dry method, semidry method and wet method.Wet desulphurization have desulfurization degree it is high, Device is reliable for operation, simple operation and other advantages, thus the existing flue gas desulfurization technique in countries in the world is mainly based on wet desulphurization. Traditional Wet Flue Gas Desulfurization Technique mainly has limestone-gypsum method, the ammonia process of desulfurization, sodium alkali desulfurization etc..Limestone-gypsum method is run Reliability is high, and application is wider, but capital expenditure is big, is easy fouling and clogging pipeline, and operating cost is high, and by-product is low-grade stone Cream, the value for recycling and utilizing are low；The ammonia process of desulfurization can be used for producing the agrochemical of high added value, but absorbent ammonia price is high Expensive, operating cost is high, and there are the escaping of ammonia to cause secondary pollution；Sodium alkali desulfurization domestic application it is most be Bell's lattice EDV The rapids of technology and sinopec rushes Venturi wet-process dedusting sodium method desulfurization technology, but main problem existing for the sulfur method is lye The high concentration saline sewage that consumption is big, discharges is difficult to handle, in line to be impacted to water ecological setting, if crystallization recycling High-purity sodium sulfite then needs largely to consume steam, causes energy consumption and processing cost unprecedented soaring.
Renewable flue gas desulfurization technique has SO in recovered flue gas2, absorbent regeneration the advantages that recycling, given birth to from cleaning The angle of production and circular economy is set out, and renewable flue gas desulfurization technique will become the trend of future development.The principle of the technology It is the SO absorbed using absorbent in flue gas2, formed and be rich in SO2Rich absorbing liquid, then by rich absorbing liquid heating regenerate, Release the SO of high concentration2For producing the high value-added products such as sulphur, the absorbent after regeneration recycles.
Absorbent used in renewable flue gas desulfurization technique is divided into organic solvent and inorganic solvent two major classes.Canada Cansolv techniques are using organic amine solvent as flue gas desulfurization absorbent；The Labsorb techniques of Bleco companies of the U.S. use phosphorus Hydrochlorate is as flue gas desulfurization absorbent；CN200910237877.1 discloses a kind of ionic liquid as flue gas desulfurization absorbent； CN201210449283.9 discloses a kind of renewable flue gas desulfurization absorbent of diamine compounds as main body； CN201410134925.5 discloses a kind of organic amine salt aqueous solution as flue gas desulfurization absorbent；CN201510654174.4 is public A kind of sulfur removal technology is opened, using one or more works in citrate buffer, phosphate buffer, organic amine buffer solution For flue gas desulfurization solvent；CN2008102097345, which is disclosed, a kind of uses sodium sulfite as renewable flue gas desulfurization absorbent Method.
Since most of coal-burning boiler and catalytic cracking unit are built according to pervious old plant, do not examined when building Considering flue gas needs further deep desulfuration, thus enough construction lands are not reserved to flue gas desulfurization when building, Flue gas desulfurization device need to be created in existing limited region or old device is transformed.Above-mentioned renewable flue gas desulfurization technique It is both needed to that Analytic Tower/regenerator/decomposition tower is separately provided, so that rich absorbent regenerates, flow is longer, and equipment is more, floor space It is larger, seriously restrict construction and the upgrading of dust-removing desulfurating apparatus, partial devices and coal-burning boiler are in default of enough Space can not upgrading, cause flue gas emission index cannot be satisfied existing national standards be forced stop work or demolish rebuild.Thus, The renewable flue gas desulfurization technique that urgently development process is short, equipment is few, floor space is few.
After wet type fume sweetening device is gone into operation, the flue gas of smoke stack emission forms the " white cigarette up to hundreds of meters or even several kilometers Long queue " brings strong visual impact, especially winter " white cigarette long queue " phenomenon particularly evident to people.In addition, a large amount of steam from Chimney direct emission causes the waste of water resource in air.Thus, it would be highly desirable to develop a kind of desulfurization with depth defrosting function Device and method.
Invention content
In view of the deficiencies of the prior art, a kind of flue gas desulfurization regeneration integrated tower of present invention offer and Regeneratable wet flue gas are de- Sulphur method, flue gas desulfurization of the invention regeneration integrated tower integrate flue gas desulfurization and regeneration of absorption solution, realize SO in flue gas2 It recycles and the depth demisting of flue gas, is greatly decreased " white cigarette phenomenon " after flue gas emission, the method for the present invention flow is short, equipment Less, operating cost is low, has broad application prospects.
The flue gas desulfurization of the present invention regenerates integrated tower, is from top to bottom followed successively by flue gas emission area, mist eliminating zone, two level spray Liquid bath area, level-one spraying zone and regeneration of absorption solution area are held by area；The regeneration of absorption solution area passes through vertical partition board I, partition board II And partition board III is followed successively by preheating zone, stripping zone and liquid collecting zone by left-to-right, is connected to level-one spraying zone at the top of preheating zone, partition board I Bottom opening makes preheating zone be connected to stripping zone, and the height of partition board II is less than the height of partition board I, stripping zone and liquid collecting zone by every The space on the tops plate II is connected to, by partition board III that stripping zone and liquid collecting zone and spraying zone is complete at the top of stripping zone and liquid collecting zone It separates.
The both ends partition board III are connect with partition board I and stripping zone liquid collecting zone tower wall respectively, and partition board I is connect with partition board III The angle at place is generally 45 ~ 165 °, preferably 120 ~ 150 °.It is close between partition board I, the partition board II and partition board III and tower wall Envelope avoids the air-liquid short circuit of partition board both sides.
Open area is arranged in the bottoms partition board I, and opening area is the 2% ~ 30% of partition board I areas, and absorbing liquid can pass through Open area enters stripping zone from preheating zone；The partition board II height is the 30% ~ 80% of partition board I height, and absorbing liquid can pass through Partition board II upper areas enter liquid collecting zone from stripping zone.
The flue gas emission area is preferably connected by cone-shaped reducing with mist eliminating zone, the tower of mist eliminating zone and flue gas emission area Diameter ratio is 1.5 ~ 5；The mist eliminating zone is preferably connected by reverse taper deformation diameter with two level spraying zone, and mist eliminating zone is sprayed with two level The tower diameter ratio in area is 1.2 ~ 3；The level-one spraying zone is preferably connected by cone-shaped reducing with regeneration of absorption solution area, absorbing liquid The tower diameter ratio of renewing zone and level-one spraying zone is 1 ~ 3.
The flue gas emission area is generally the chimney structure in conventional smoke-gas wet desulfurization method, the chimney bottom Portion is connected with mist eliminating zone tower body, is preferably connected with mist eliminating zone tower body by cone-shaped reducing, and exhanst gas outlet is arranged in chimney top；It is excellent It is selected in chimney top setting outer sleeve, the outer sleeve is the tubular structure of upper and lower opening, can be cylindric or cone cylinder shape, Outer sleeve upper edge is higher by chimney top certain distance, generally 0.2~10m, preferably 0.5~5m, and the lower edge of outer sleeve is less than The upper edge of chimney, preferably shorter than 0.5 ~ 5m of chimney upper edge；It is annular space between the outer sleeve and chimney, preferably bottom is opened 1.01~1.2 times of a diameter of chimney top opening diameter of mouth.The flue gas enters outer sleeve from chimney top, from outer sleeve Top is discharged, and the gas velocity of flue gas is higher, can generate negative pressure between chimney and outer sleeve when flowing through outer sleeve, air is in negative pressure Suction under flow through between chimney and outer sleeve annular space enter outer sleeve top, air is in outer sleeve and flue gas Together from outer sleeve top discharge after mixing, flue gas has just been sufficiently mixed with air before leaving outer sleeve top discharge, greatly Width reduces " white cigarette " production quantity.
Demister is arranged in the mist eliminating zone, and the drop for removing flue gas carrying, the demister can be eddy flow One or more of demister, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
The two level spraying zone is arranged one or more layers spray pipe, when Multi-layer sprinkling pipeline is set, spray pipe it Between distance be 0.5 ~ 5m, preferred distance be 1 ~ 2.5m；The spray pipe connects lye pipeline I, is arranged on spray pipe There are multiple atomizers；For lye to be atomized, the droplet after atomization contacts the two level spraying zone with flue gas adverse current, takes off Except the sulfur dioxide carried in flue gas.
Several riseies are arranged in the liquid bath area of holding, and flue gas enters two level spray from level-one spraying zone by riser Area；Described holds the one or more overflow pipes of liquid bath area setting, and overflow pipe height is less than riser height, holds the lye in liquid bath Enter level-one spraying zone by overflow pipe.
The liquid bath area tower wall side of holding is separately connected alkaline solution line I, fresh water pipeline；The alkaline solution Flow control valve is set on pipeline I, for hold in liquid bath fill alkaline solution adjust its pH value；On the fresh water pipeline Be arranged regulating valve, for hold in liquid bath fill fresh water adjust liquid collecting zone liquid level；The liquid bath area bottom of holding is connected with alkali Liquid extracts pipeline out.
At least two layers of spray pipe is arranged in the level-one spraying zone, and the distance between spray pipe is 0.5 ~ 5m, preferably Distance is 1 ~ 2.5m；The spray pipe connects poor absorbing liquid pipeline I, and multiple atomizers are provided on spray pipe；Institute For poor absorbing liquid to be atomized, the droplet after atomization contacts the level-one spraying zone stated with flue gas adverse current, removes and is carried in flue gas Sulfur dioxide.
Set of heat exchange tubes is arranged in the preheating zone, and the lower end of set of heat exchange tubes is fixed on the bottom of tower of preheating zone and flue gas pipeline connects Logical, the upper outlet end of set of heat exchange tubes leads to preheating zone ullage；The top at the set of heat exchange tubes upper outlet end is arranged Umbrella crown shape baffle enters set of heat exchange tubes to avoid the droplet of spray.
The set of heat exchange tubes is by an at least set of heat exchange tubes at heat exchanger tube can be light pipe, fins pipe, screwed pipe, wave One or more of line pipe, band pipe, shaped telescopic tube, spiral grooved tube or tube with high flux etc.；The set of heat exchange tubes is changed by one When heat pipe forms, heat exchanger tube is twist arranged to increase heat exchange area, and heat exchanger tube is fixed in bottom of tower and tower wall to subtract The vibration of few heat exchanger tube extends its service life；The heat exchanger tube by two or two or more set of heat exchange tubes at when, heat exchange It is fixed to each other, avoids impinging one another between heat exchanger tube between pipe.The quantity of the heat exchanger tube setting can be according to flue gas stream Amount and smoke inlet temperature are adjusted, and the heat exchanger tube is immersed under the richness absorbing liquid liquid level of preheating zone, generally through changing The temperature of rich absorbing liquid after heat pipe heat exchanging is 60 ~ 95 DEG C；Heat exchanger tube cross-sectional area sum is the 1 ~ 2 of flue gas pipeline cross-sectional area Times, to reduce flue gas flow rate, and then reduce the pressure drop of set of heat exchange tubes.
The stripping zone lower part is provided with stripped vapor distributor pipe, and stripping zone is fixed in the lower end of stripped vapor distributor pipe Bottom of tower；The stripped vapor distributor pipe is connected to steam pipe line, be provided on stripped vapor distributor pipe it is several vertically upward Nozzle；The stripping zone uses stripped vapor as heat medium, and rich absorbing liquid is heated in stripping zone and is decomposited with dioxy Regeneration gas based on change sulphur and steam, forms poor absorbing liquid.
Liquid collecting zone tower wall side connection alkaline solution line II, outer comb line and the liquid level gauge；The liquid collecting zone For collecting the poor absorbing liquid after regenerating；Flow control valve is set on the alkaline solution line II, is used for poor absorbing liquid Middle filling alkaline solution adjusts its pH value；The outer comb line is used to arrange to reduce in poor absorbing liquid outside a small amount of poor absorbing liquid Sulfate concentration；Gas vent is arranged in tower wall above the liquid collecting zone, for connecting regeneration gas pipeline；The liquid collecting Area bottom is connected with poor absorbing liquid pipeline II, for connecting bottom of tower circulating pump.
Present invention simultaneously provides a kind of Regeneratable wet fuel gas desulfurizing method, above-mentioned flue gas desulfurization is used in this method Regenerate integrated tower.
The Regeneratable wet fuel gas desulfurizing method of the present invention, including the following contents：Flue gas after dedusting through flue gas pipeline from The preheating zone bottom of flue gas desulfurization regeneration integrated tower enters set of heat exchange tubes, from set of heat exchange tubes after exchanging heat with the rich absorbing liquid of preheating zone Top enters level-one spraying zone, flue gas and most of titanium dioxide in the poor absorbing liquid counter current contacting removing flue gas of level-one spraying zone Sulphur enters two level spraying zone across the flue gas of level-one spraying zone, and deep desulfuration is carried out in two level spraying zone and lye counter current contacting, Purified flue gas enters after outer sleeve is sufficiently mixed with air from the chimney top in flue gas emission area at the top of flue gas emission area Discharge；Enter stripping zone below the partition board I between preheating zone and stripping zone with the rich absorbing liquid after flue gas heat exchange, by steam plus The regeneration gas based on sulfur dioxide and steam is thermally decomposed out, poor absorbing liquid is formed；Impetus of the poor absorbing liquid in steam It is lower to enter liquid collecting zone, it is arranged outside a small amount of poor absorbing liquid, remaining poor absorbing liquid is extracted out from the bottom of liquid collecting zone, and one is entered after cooling Grade spraying zone recycles, gas vent discharge of the regeneration gas through stripping zone top.
In the method for the present invention, the flue gas is fire coal boiler fume, coal-fired plant flue gas, catalytic cracking catalyst regeneration One or more of flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas.
In the method for the present invention, the alkaline solution include sodium hydroxide solution, potassium hydroxide solution, sodium carbonate liquor, One or more of solution of potassium carbonate, sodium sulfite solution or potassium sulfite solution etc..
In the method for the present invention, the liquid level of the liquid collecting zone is held by entering in the middle part of tower body on the fresh water pipeline of liquid bath Regulating valve controlled.
In the method for the present invention, is arranged outside a small amount of poor absorbing liquid, be primarily due to sulfite solution in flue gas desulfurization It can be sulfate by the dioxygen oxidation in flue gas to regenerate small part sulphite in integrated tower inner cyclic process, and sulfate loses suction The ability of sulfur dioxide is received, thus it is in device operational process that row outside a small amount of poor absorbing liquid is dense to reduce the sulfate in lean solution Degree, poor absorbing liquid enter subsequent processing units, can be used for crystallization and prepare sodium sulfite or potassium sulfite, sodium sulphate or potassium sulfate etc. Product, also can oxidized rear qualified discharge.
In the method for the present invention, poor absorbing liquid pH value control is followed in 6.0 ~ 7.5, pH on-line detectors positioned at bottom of tower On ring pump intake pipeline, the pH value of poor absorbing liquid is controlled by controlling the alkaline solution flow into liquid collecting zone.
In the method for the present invention, the lye of sulfur dioxide is absorbed in two level spraying zone, after being mixed with fresh water, fresh lye It extracts out from liquid bath bottom is held, is recycled after the pressurization of stage casing circulating pump.The lye pH value control exists in 5.0 ~ 7.5, pH Line detector is located on the pump entry pipeline of stage casing, and lye is controlled into the fresh flux of alkaline liquor of liquid bath is held by controlling PH value.
In the method for the present invention, the temperature after the rich absorbing liquid and flue gas heat exchange is generally 60 ~ 95 DEG C, rich absorbing liquid into Enter stripping zone, the temperature after being heated by steam is generally 70 ~ 100 DEG C.
In the method for the present invention, the stripping zone pressure is controlled in -200 ~ 200kPa（Gauge pressure）, preferably -200 ~ 0kPa（Table Pressure）, stripping zone pressure controlled by the variable-frequency motor of air-introduced machine inlet vane aperture or air-introduced machine.
In the method for the present invention, regeneration gas enters condensation under the action of air-introduced machine by the gas vent on stripping zone top Device, by under the condensate moisture of carrying in condenser, sulfur dioxide enters subsequent sulfur recovery facility or Sulphuric acid device It is recycled, the suction line that condensed water enters bottom of tower circulating pump continues cycling through use.
Compared with the prior art, the advantages of the present invention are as follows：
1, the present invention is in flue gas desulfurization regeneration integrated tower lower part setting regeneration of absorption solution area, by three pieces of partition boards by regeneration of absorption solution Divide into preheating zone, stripping zone and liquid collecting zone；Open area is arranged in the vertical clapboard bottom in regeneration of absorption solution area center, and richness absorbs Liquid enters stripping zone under the promotion of the liquid level difference of vertical clapboard both sides from preheating zone；Rich absorbing liquid regenerates to obtain height in stripping zone The SO of added value2Gas can be used as the raw material of follow-up sulphur recovery or Sulphuric acid device, realize SO in flue gas2Recycling profit With.
2, flue gas is entered by preheating zone bottom in the present invention, and high-temperature flue gas exchanges heat with rich absorbing liquid, takes full advantage of The waste heat of high-temperature flue gas significantly reduces the dosage of stripped vapor, realizes UTILIZATION OF VESIDUAL HEAT IN, energy-saving purpose；Flue gas with Temperature is greatly reduced after rich absorbing liquid heat exchange, thus poor absorbing liquid and lye moisture evaporation amount during washing flue gas substantially drop Low, the load of demister is substantially reduced, and exhaust gas temperature reduces, and the moisture in flue gas also lowers therewith, after flue gas emission " white cigarette " phenomenon is obviously cut down, and the depth demisting of desulfurization fume is realized.
3, reverse taper deformation diameter is arranged in the present invention between mist eliminating zone and two level spraying zone, advantageously reduces mist eliminating zone gas Speed, demisting efficiency of the raising flue gas in mist eliminating zone；Cone-shaped reducing is arranged with mist eliminating zone in flue gas emission area, is conducive to improve flue gas Flow velocity, the gas velocity of flue gas is bigger, and it is higher that flue gas leaves the rising height behind flue gas emission area, is more conducive to the diffusion of flue gas, Thus plume is shorter.
4, flue gas desulfurization of the invention regeneration integrated tower flue gas emission area is using the structure of " chimney+outer sleeve ", flue gas warp Negative pressure is generated after crossing the acceleration of mist eliminating zone and cone-shaped reducing, when flue gas flows through outer sleeve to suck outside air, flue gas and sky Gas be sufficiently mixed in outer sleeve after from outer sleeve top discharge, significantly reduce " white cigarette " production quantity.
5, the present invention completes flue gas desulfurization and absorbing liquid steam stripping regeneration in a tower, each functional area coordinated, Technological process is short, and floor space is greatly reduced, and significantly reduces the expense needed for plant construction, transformation.
Description of the drawings
Fig. 1 is that flue gas desulfurization of the present invention regenerates integral structure schematic diagram.
Fig. 2 is demarcation strip A of the present invention to structural schematic diagram.
Fig. 3 is demarcation strip B of the present invention to structural schematic diagram.
Fig. 4 is demarcation strip C of the present invention to structural schematic diagram.
Fig. 5 is demister structural schematic diagram of the present invention.
Fig. 6 is the schematic cross-section of riser I tangential flow guidings plate and straight tube hyoplastron in demister of the present invention.
Fig. 7 is the tangential flow guiding plate that cylindrical protrusions are carried in demister of the present invention.
Fig. 8 is the cylindrical protrusions that structure is threaded in demister of the present invention.
Fig. 9 is present invention process flow diagram.
In figure：1- flue gas emissions area；2- cone-shaped reducings；3- mist eliminating zones；4- reverse taper deformation diameters；5- two level spraying zones； 6- holds liquid bath area；7- level-one spraying zones；8- regeneration of absorption solution area；The preheating zones 9-；The stripping zones 10-；The liquid collecting zones 11-；12- demistings Device；15- riseies；16- overflow pipes；17- holds liquid bath；18- bullet reducings；19- gas vents；20- partition boards I；21- partition boards II；22- partition boards III；23- stripped vapor distributor pipes；24- set of heat exchange tubes；25- umbrella crown shape baffles；The stage casings 26- circulating pump；27- towers Bottoming cycle pumps；28- coolers；29- air-introduced machines；30- condensers；31- chimneys；32- outer sleeves；
Wherein, 5-1 lye pipeline I；6-1- fresh solution pipelines I；The fresh water pipelines of 6-2-；6-3- lye extracts pipeline out；7-1- Poor absorbing liquid pipeline I；9-1- flue gas pipelines；10-1- steam pipe lines；11-1- regeneration gas pipelines；11-2- condensate pipings； The outer comb lines of 11-3-；11-4- alkaline solution lines II；The poor absorbing liquid pipeline II of 11-5-；11-6- liquid level gauges；12-1- tower trays； 12-2- riseies II；12-3- bearings；12-4- riseies I；12-5- items stitch；12-6- tangential flow guiding plates；12-7- covers plate； 12-8- protrusions；12-9- straight tubes；13-1- level-one spraying zone spray tubes；13-2- two level spraying zone spray tubes；14-1- level-ones spray Area's atomizer；14-2- two level spraying zone atomizers；.
Specific implementation mode
Below in conjunction with drawings and examples, the present invention will be described in detail.
The flue gas desulfurization of the present invention regenerates integrated tower, is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, two level spray Liquid bath area 6, level-one spraying zone 7 and regeneration of absorption solution area 8 are held by area 5；The regeneration of absorption solution area 8 passes through vertical partition board I 20, partition board II 21 and partition board III 22 is followed successively by preheating zone 9, stripping zone 10 and liquid collecting zone 11,9 top of preheating zone from left to right It is connected to level-one spraying zone 7,20 bottom openings of partition board I make preheating zone 9 be connected to stripping zone 10, and the height of partition board II 21 is less than The height of partition board I 20, stripping zone 10 are connected to liquid collecting zone 11 by the space on 21 tops partition board II, stripping zone 10 and liquid collecting zone 11 tops are completely separated by stripping zone 10 and liquid collecting zone 11 and level-one spraying zone 7 by partition board III 22.
22 both ends partition board III are connect with partition board I 20 and stripping zone 10,11 tower wall of liquid collecting zone respectively, partition board I 20 are generally 45 ~ 165 °, preferably 120 ~ 150 ° with the angles of 22 junctions partition board III.Partition board I 20, the partition board II It is sealed between 21 and partition board III 22 and tower wall, avoids the air-liquid short circuit of partition board both sides.
Open area is arranged in 20 bottoms partition board I, and opening area is the 2% ~ 30% of 20 areas of partition board I, absorbing liquid Stripping zone 10 can be entered from preheating zone 9 by open area；21 height of partition board II be 20 height of partition board I 30% ~ 80%, absorbing liquid can enter liquid collecting zone 11 by 21 upper areas of partition board II from stripping zone 10.
The flue gas emission area 1 is preferably connected by cone-shaped reducing 2 with mist eliminating zone 3, mist eliminating zone 3 and flue gas emission area 1 tower diameter ratio is 1.5 ~ 5；The mist eliminating zone 3 is preferably connected by reverse taper deformation diameter 4 with two level spraying zone 5, mist eliminating zone 3 Tower diameter ratio with two level spraying zone 5 is 1.2 ~ 3；The level-one spraying zone 7 preferably passes through cone deformation with regeneration of absorption solution area 8 Diameter 18 is connected, and the tower diameter ratio of regeneration of absorption solution area 8 and level-one spraying zone 7 is 1 ~ 3.
The flue gas emission area 1 is generally 31 structure of chimney in conventional smoke-gas wet desulfurization method, the cigarette 31 bottom of chimney is connected with 3 tower body of mist eliminating zone, is preferably connected with 3 tower body of mist eliminating zone by cone-shaped reducing 2,31 top setting of chimney Exhanst gas outlet；It is preferred that outer sleeve 32 is arranged at the top of chimney 31, the outer sleeve 32 is the tubular structure of upper and lower opening, can be with It is higher by 31 top certain distance of chimney, generally 0.2~10m, preferably 0.5 for cylindric or cone cylinder shape, 32 upper edge of outer sleeve ~5m, the lower edge of outer sleeve 32 are less than the upper edge of chimney 31, preferably shorter than 31 0.5 ~ 5m of upper edge of chimney；The outer sleeve 32 with It is annular space, preferably 1.01~1.2 times of a diameter of 31 open top diameter of chimney of bottom opening between chimney 31.Described Flue gas enters outer sleeve 32 from 31 top of chimney, and from 32 top discharge of outer sleeve, the gas velocity of flue gas is higher, is flowing through outer sleeve 32 When negative pressure can be generated between chimney 31 and outer sleeve 32, air flows through chimney 31 and outer sleeve 32 under the suction of negative pressure Between annular space enter 32 top of outer sleeve, air mix with flue gas in outer sleeve 32 after together at the top of outer sleeve 32 Discharge, flue gas have just been sufficiently mixed with air before leaving 32 top discharge of outer sleeve, significantly reduce " white cigarette " production quantity.
Demister 12 is arranged in the mist eliminating zone 3, the drop for removing flue gas carrying, and the demister can be rotation Flow one or more of demister, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
One or more layers spray tube 13-2 is arranged in the two level spraying zone 5, when Multi-layer sprinkling pipe 13-2 is set, spray tube The distance between 13-2 is 0.5 ~ 5m, and preferred distance is 1 ~ 2.5m；The spray tube 13-2 connection lye pipeline I 5-1, spray Multiple atomizer 14-2 are provided on shower pipe 13-2；The two level spraying zone 5 is for lye to be atomized, the small liquid after atomization Drop is contacted with flue gas adverse current, removes the sulfur dioxide carried in flue gas.
Several riseies 15 are arranged in the liquid bath area 6 of holding, and flue gas enters two level from level-one spraying zone 7 by riser 15 Spraying zone 5；One or more overflow pipes 16 are arranged in the liquid bath area 6 of holding, and 16 height of overflow pipe is held less than 15 height of riser Lye in liquid bath 17 enters level-one spraying zone 7 by overflow pipe 16.
The 6 tower wall side of liquid bath area of holding is separately connected alkaline solution line I 6-1, fresh water pipeline 6-2；Described Flow control valve is set on alkaline solution line I 6-1, for hold in liquid bath 17 fill alkaline solution adjust its pH value；It is described Fresh water pipeline 6-2 on regulating valve is set, for hold in liquid bath 17 fill fresh water to adjust 11 liquid level of liquid collecting zone；It is described 6 bottom of liquid bath area of holding be connected with lye extraction pipeline 6-3.
At least two layers of spray tube 13-1 is arranged in the level-one spraying zone 7, and the distance between spray tube 13-1 is 0.5 ~ 5m, Preferred distance is 1 ~ 2.5m；It is provided on spray tube 13-1 the connections poor absorbing liquid pipeline I 7-1, spray tube 13-1 multiple Atomizer 14-1；For poor absorbing liquid to be atomized, the droplet after atomization connects the level-one spraying zone 7 with flue gas adverse current It touches, removes the sulfur dioxide carried in flue gas.
Set of heat exchange tubes 24 is arranged in the preheating zone 9, and bottom of tower and the flue gas of preheating zone 9 are fixed in the lower end of set of heat exchange tubes 24 Pipeline 9-1 connections, the upper outlet end of set of heat exchange tubes 24 leads to 9 ullage of preheating zone；24 top of set of heat exchange tubes goes out The top setting umbrella crown shape baffle 25 at mouth end, enters set of heat exchange tubes 24 to avoid the droplet of spray.
The set of heat exchange tubes 24 by an at least set of heat exchange tubes at, heat exchanger tube can be light pipe, fins pipe, screwed pipe, One or more of bellows, band pipe, shaped telescopic tube, spiral grooved tube or tube with high flux etc.；The set of heat exchange tubes 24 is by one Root set of heat exchange tubes at when, heat exchanger tube is twist arranged to increase heat exchange area, and heat exchanger tube is fixed on bottom of tower and tower wall Vibration to reduce heat exchanger tube prolongs the service life；The heat exchanger tube by two or two or more set of heat exchange tubes at when, change It is fixed to each other, avoids impinging one another between heat exchanger tube between heat pipe；The quantity of the heat exchanger tube setting can be according to flue gas Flow and smoke inlet temperature are adjusted, and the heat exchanger tube is immersed under the richness absorbing liquid liquid level of preheating zone, general to pass through The temperature of rich absorbing liquid after heat exchanger tube heat exchange is 65 ~ 95 DEG C；Heat exchanger tube cross-sectional area sum is flue gas pipeline 9-1 cross-sectional areas 1 ~ 2 times, to reduce flue gas flow rate, and then reduce the pressure drop of set of heat exchange tubes 24.
10 lower part of stripping zone is provided with stripped vapor distributor pipe 23, and the lower end of stripped vapor distributor pipe 23 is fixed on The bottom of tower of stripping zone 10；The stripped vapor distributor pipe 23 is connected to steam pipe line 10-1, is set on stripped vapor distributor pipe 23 It is equipped with several nozzles vertically upward；The stripping zone 10 uses stripped vapor as heat medium, and rich absorbing liquid is stripping The heated regeneration gas decomposited based on sulfur dioxide and steam in area 10, forms poor absorbing liquid.
The liquid collecting zone 11 is used to collect the poor absorbing liquid after regeneration；11 tower wall side of the liquid collecting zone connection alkalinity Solution pipeline II 11-4, outer comb line 11-3 and liquid level gauge 11-6；Flow is set on the alkaline solution line II 11-4 Regulating valve adjusts its pH value for filling alkaline solution into poor absorbing liquid；The outer comb line 11-3 is used for will be a small amount of poor It is arranged outside absorbing liquid to reduce the sulfate concentration in poor absorbing liquid；Gas vent 19 is arranged in the 11 top tower wall of liquid collecting zone, For connecting regeneration gas pipeline 11-1；11 bottom of liquid collecting zone is connected with poor absorbing liquid pipeline II 11-5, for connecting Bottom of tower circulating pump 27.
Embodiment
Flue gas desulfurization regenerates integrated tower, is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, two level spraying zone 5, holds liquid Slot area 6, level-one spraying zone 7 and regeneration of absorption solution area 8；Flue gas emission area 1 is preferably connected by cone-shaped reducing 2 with mist eliminating zone 3, The tower diameter ratio in mist eliminating zone 3 and flue gas emission area 1 is 2.5 ~ 5；Mist eliminating zone 3 preferably passes through reverse taper deformation diameter 4 with two level spraying zone 5 It is connected, the tower diameter ratio of mist eliminating zone 3 and two level spraying zone 5 is 1.5；Level-one spraying zone 7 preferably passes through cone with regeneration of absorption solution area 8 Deformation diameter 18 is connected, and the tower diameter ratio of regeneration of absorption solution area 8 and level-one spraying zone 7 is 1.5.
Regeneration of absorption solution area 8 is followed successively by pre- from left to right by vertical partition board I 20, partition board II 21 and partition board III 22 Hot-zone 9, stripping zone 10 and liquid collecting zone 11,9 top of preheating zone are connected to level-one spraying zone 7, and 20 bottom openings of partition board I make preheating Area 9 is connected to stripping zone 10, and opening area is the 10% of 20 areas of partition board I；The height of partition board II 21 is the height of partition board I 20 60%, stripping zone 10 is connected to liquid collecting zone 11 by the space on 21 tops partition board II, and stripping zone 10 and the top of liquid collecting zone 11 are logical Cross partition board III 22 stripping zone 10 and liquid collecting zone 11 and level-one spraying zone 7 is completely separated.
22 both ends partition board III are connect with partition board I 20 and stripping zone 10,11 tower wall of liquid collecting zone respectively, partition board I 20 with every The angle of 22 junctions plate III is 120 °；It seals, avoids between partition board I 20, partition board II 21 and partition board III 22 and tower wall The air-liquid short circuit of partition board both sides.
31 structure of chimney in conventional smoke-gas wet desulfurization method is arranged in flue gas emission area 1, and 31 bottom of chimney passes through cone Bodily form reducing 2 is connected with 3 tower body of mist eliminating zone, outer sleeve 32 is arranged at 31 top of chimney, outer sleeve 32 is the cylinder of upper and lower opening Shape structure, 32 upper edge of outer sleeve are higher by 31 top 5m of chimney, and the lower edge of outer sleeve 32 is less than 31 0.5 ~ 5m of upper edge of chimney, outer sleeve 1.1 times of the 31 open top diameter of a diameter of chimney of 32 bottom openings.
Demister 12 is arranged in the mist eliminating zone 3, it is preferred that uses demister 12 as shown in Fig. 5 ~ 8.Demister 12 wraps Riser I 12-4, riser II 12-2 and straight tube 12-9 are included, riser I 12-4 and riser II 12-2 pass through bearing 12- 3 connections, straight tube 12-9 is arranged in the outside of riser I 12-4 and riser II 12-2, and with riser I 12-4, II 12- 2 on the same axis；Riser II 12-2 are fixed on tower tray 12-1；The top setting capping plate 12-7 of riser I 12-4, Several seam 12-5 are provided in the circumference of riser I, provided circumferentially about are cut in the riser I 12-4 for stitching 12-5 close to each item To deflector 12-6, several cylindrical protrusions 10 are set on tangential flow guiding plate, protrusion 12-8 is set on the inner wall of straight tube 12-9.
The size of item seam 12-5 is opened up on the riser tube wall, and need can be needed or designed according to actual operating mode It asks, is determined by those skilled in the art.As the item seam 12-5 height can be 20~500mm, preferably 200~ 350mm；The width that item stitches 12-5 can be 20~120mm, preferably 50~80mm.The area that always cracks of the item seam, generally Can be 3~5 times of riser sectional area.It is equipped with tangential flow guiding plate 12-6, and tangential flow guiding plate with item seam 12-5 connected positions The direction of rotation of 12-6 is consistent, and tangential flow guiding plate 12-6 mainly plays drainage and baffling.The angle that tangential flow guiding plate 12-6 is tilted Degree α is generally 5 °~45 °, preferably 15 °~30 °.Riser top is equipped with capping plate 12-7, with riser tube wall airtight connection.
In the demister 12 of the present invention, wherein the upper end of straight tube 12-9, which is higher than, covers plate 12-7, and the lower edge of straight tube 12-9 Apart from tower tray 12-1 certain distances.The lower edge of straight tube 12-9 should be less than the lower edge of item seam 12-5.Straight tube 12-9 lower edges are away from a liter gas The vertical range that pipe item stitches 12-5 lower edges can be 20~260mm, preferably 50~80mm.Straight tube 12-9 diameters can be riser 1.1 times of diameter~1.6 times, preferably 1.1 times~1.2 times.The height of straight tube 12-9 can be that riser item stitches 12-5 height 1.3 times~2 times.Height of the straight tube 12-9 lower edges away from tower tray 12-1 can be 5~100mm, preferably 20~50mm.
In the demister 12 of the present invention, the inner surface of straight tube 12-9（Inner wall）Upper setting protrusion 12-8, raised 12-8 with it is straight The axis of cylinder 12-9 is parallel, or can form an angle with axis, and such as angle can be 10 °~45 °, preferably 15 °~ 25°.The section of raised 12-8 can be rectangle, triangle or arc-shaped, and preferably rectangular in of the invention, i.e., protrusion is preferably tongue Plate.As in figure 6, raised 12-8 is hyoplastron.Raised 12-8 is generally uniformly distributed on the inner surface of straight tube, and quantity is to rise gas Pipe item stitches 1.5~3 times of quantity.The direction of rotation of several protrusion 12-8 is consistent, the direction of rotation phase with tangential flow guiding plate 12-6 It is same or rather, it is preferred to opposite with the direction of rotation of tangential flow guiding plate 12-6.
In the demister 12 of the present invention, several cylindrical protrusions 12-8 are set on tangential flow guiding plate 12-6, preferably with The cylindrical protrusions of helicitic texture, cylindrical protrusions 12-8 are uniformly distributed on deflector, cylindrical protrusions 12-8 occupied areas Generally the 10% ~ 50% of tangential flow guiding plate 12-6 areas.
Two layers of spray tube 13-2 is arranged in two level spraying zone 5, and the distance between spray tube 13-2 is 2m, spray tube 13-2 connections It is provided with multiple atomizer 14-2 on lye pipeline I 5-1, spray tube 13-2.
It holds liquid bath area 6 and several riseies 15 and an overflow pipe 16 is set, 16 height of overflow pipe is less than 15 height of riser. It holds 6 tower wall side of liquid bath area and is separately connected alkaline solution line I 6-1, fresh water pipeline 6-2, it is alkaline solution line I 6-1, new It is both provided with flow control valve on fresh water pipeline 6-2,6 bottom of liquid bath area is held and is connected with lye extraction pipeline 6-3.
Two layers of spray tube 13-1 is arranged in level-one spraying zone 7, and the distance between spray tube 13-1 is 2m, spray tube 13-1 connections It is provided with multiple atomizer 14-1 on poor absorbing liquid pipeline I 7-1, spray tube 13-1.
Set of heat exchange tubes 24 is arranged in preheating zone 9, and bottom of tower and the flue gas pipeline 9- of preheating zone 9 are fixed in the lower end of set of heat exchange tubes 24 1 connection, the upper outlet end of set of heat exchange tubes 24 lead to 9 ullage of preheating zone, and set of heat exchange tubes is set above 24 upper outlet end Set umbrella crown shape baffle 25.
Set of heat exchange tubes 24 is by two set of heat exchange tubes at being fixed to each other between heat exchanger tube, heat exchanger tube is fins pipe, and heat exchanger tube is in Helix shape is simultaneously fixed in bottom of tower and tower wall, and heat exchanger tube is immersed under the richness absorbing liquid liquid level of preheating zone, and heat exchanger tube is transversal The sum of area is 1.5 times of flue gas pipeline 9-1 cross-sectional areas, to reduce flue gas flow rate, and then reduces the pressure drop of set of heat exchange tubes 24.
10 lower part of stripping zone is provided with stripped vapor distributor pipe 23, and stripping zone is fixed in the lower end of stripped vapor distributor pipe 23 10 bottom of tower, stripped vapor distributor pipe 23 are connected to steam pipe line 10-1, are provided on stripped vapor distributor pipe 23 several vertical Upward nozzle.
11 tower wall side of liquid collecting zone connects alkaline solution line II 11-4, outer comb line 11-3 and liquid level gauge 11-6, alkalinity Flow control valve is set on solution pipeline II 11-4, and gas vent 19 is arranged in 11 top tower wall of liquid collecting zone, for connecting regeneration gas Fluid line 11-1,11 bottom of liquid collecting zone is connected with poor absorbing liquid pipeline II 11-5, for connecting bottom of tower circulating pump 27.
The Regeneratable wet fuel gas desulfurizing method of the present invention, including the following contents：
（1）9 bottom of preheating zone that flue gas after dedusting regenerates integrated tower through flue gas pipeline 9-1 from flue gas desulfurization enters set of heat exchange tubes 24, level-one spraying zone 7 is entered after exchanging heat with rich absorbing liquid, flue gas and the poor absorbing liquid counter current contacting of level-one spraying zone 7 remove cigarette The most of sulfur dioxide carried in gas, across level-one spraying zone 7 flue gas by hold the air rising hole being arranged on liquid bath 17 15 into Enter two level spraying zone 5, deep desulfuration is carried out in two level spraying zone 5 and circulation alkali liquor counter current contacting, the flue gas of entrained drip is from tower Disk 12-1 lower spaces enter riser II 12-2, and flue gas in uphill process, carry liquid phase secretly and rise by flue gas, meets capping plate 12- Gas phase flow direction changes after 7（Horizontal or level of approximation direction is changed to by ascent direction）, and droplet is made due to inertia It is collided, and is attached on capping plate 12-7 with capping plate 12-7, the drop of attachment becomes larger, and drop arrives greatly its own The gravity of generation be more than gas climbing power and surface tension of liquid resultant force when, drop is just divided on plate 12-7 surfaces from covering From getting off, a gas-liquid separation is completed.The line of rabbet joint outflow that the gas-liquid two-phase not detached is opened up from the tops riser I 12-4, When drop in gas phase encounters screwed cylindrical protrusions 12-8, it is attached on screw thread and assembles, and flowed down along screw thread, Under the guide functions of tangential flow guiding plate 12-6, gas phase is made to change again, the droplet not being removed is in tangential flow guiding plate The turnings 12-6 are captured by identical effect, complete another gas-liquid separation, while tangential flow guiding plate 12-6 is in gas Under the impetus of body, drive riser I 12-4 by connect bearing rotate, the rotation direction of riser I 12-4 with Tangential flow guiding plate 12-6's is oppositely oriented, makes continuously to hit outer tube inner wall everywhere from the gas after the 12-6 outflows of tangential flow guiding plate, Without being merely to hit outer tube inner wall fixed position, shaving effect is strengthened, while it is uniform in outer barrel to be more favorable to gas Distribution.Simultaneously as straight tube 12-9 inner walls are equipped with hyoplastron, and when encountering the hyoplastron on straight tube 12-9 inner walls, since airbond occurs, Gas flow direction changes again, and droplet is attached to the turning on the inner wall hyoplastron of straight tube, and drop aggregation becomes larger, edge The crack of hyoplastron and barrel flows down, and accelerates coalescence, reduces entrainment.Drop is when flowing downward, in blowing for gas Under, drop hurtles down, and realizes gas-liquid separation.Flue gas after demisting enters outer sleeve from 31 top of chimney in flue gas emission area 1 32 be sufficiently mixed with air after 1 discharge at the top of the flue gas emission area.
（2）Circulation alkali liquor, fresh water and alkaline solution（The NaOH solution of 30w%）The mixing of liquid bath 17 is held in the middle part of tower body Afterwards from the extraction of 17 bottom of liquid bath is held, enter two level spraying zone 5 after the pressurization of stage casing circulating pump 26, lye is through atomizer 14-2 mists It is contacted with flue gas adverse current after change, the sulfur dioxide absorbed in flue gas generates sodium sulfite, and reaction equation is：2NaOH+SO2→ Na2SO3+H2O；The lye for absorbing sulfur dioxide enters in the middle part of tower and holds liquid bath 17, from the overflow pipe for holding liquid bath 17 flow out from Flow downward under the action of body gravity, preheating zone 9 entered after level-one spraying zone 7, the sodium sulfite in circulation alkali liquor to The sulfur dioxide generation sodium hydrogensulfite for continuing to absorb in flue gas is contacted during lower flowing with flue gas adverse current and forms rich absorption Liquid, reaction equation are as follows：
Na2SO3+SO2+H2O →2NaHSO3
（3）A small amount of poor absorbing liquid of liquid collecting zone 11 is primarily due to absorbing liquid in cyclic process by being arranged outside outer comb line 11-3 Middle small part sodium sulfite can be sodium sulphate, 2Na by the dioxygen oxidation in flue gas2SO3 + O2→2Na2SO4Sodium sulphate loses suction The ability of sulfur dioxide is received, therefore needs outer row on a small quantity；Remaining poor absorbing liquid mixed with a small amount of NaOH solution after from the bottom of liquid collecting zone 11 Portion is extracted out, is cooled into cooler 28 after the pressurization of bottom of tower circulating pump 27, the poor absorbing liquid after cooling enters level-one Spraying zone 7, poor absorbing liquid contact after atomizer 14-1 atomizations with flue gas adverse current, and the NaOH in poor absorbing liquid absorbs in flue gas Sulfur dioxide generate sodium sulfite, the sodium sulfite in poor absorbing liquid absorbs the sulfur dioxide in flue gas and generates sodium hydrogensulfite Rich absorbing liquid is formed, reaction equation is as follows：
2NaOH+SO2→Na2SO3+H2O
Na2SO3+SO2+H2O →2NaHSO3
（4）The rich absorbing liquid for absorbing sulfur dioxide enters the preheating zone 9 of tower bottom and exchanges heat with flue gas, and rich after heat exchange is inhaled It is 65 ~ 95 DEG C to receive liquid temperature, and rich absorbing liquid enters stripping zone 10 below the demarcation strip between preheating zone 9 and stripping zone 10, It is flowed up under the impetus of stripped vapor, rich absorbing liquid is steam heated to 70 ~ 100 DEG C in stripping zone 10, rich absorbing liquid The heated regeneration gas decomposited based on sulfur dioxide and steam, forms poor absorbing liquid, and poor absorbing liquid is made in the promotion of steam The partition board II crossed under between stripping zone 10 and liquid collecting zone 11 enters liquid collecting zone 11；Sodium hydrogensulfite is by pyrolysis equation Formula is as follows：2NaHSO3→Na2SO3+SO2+H2O；Regeneration gas passes through the gas on 10 top of stripping zone under the action of air-introduced machine 29 Outlet 19 enters condenser 30, and under the condensate moisture in condenser 30 by carrying, sulfur dioxide is returned into subsequent sulphur Receiving apparatus or Sulphuric acid device are recycled, and the suction line that condensed water enters bottom of tower circulating pump 27 continues cycling through use.
Flue gas flow after certain enterprise's dedusting is 200000Nm3/ h, flue-gas temperature are 168 DEG C, SO in flue gas2Content is 1100mg/Nm3, flue gas emission mouth SO2Content is 25mg/Nm3, SO in flue gas2Removal efficiency is 97.73%.
Rich absorbing liquid is increased to 73 DEG C with temperature after flue gas heat exchange and enters stripping zone, the condensed device of regeneration gas after stripping SO is obtained after condensation2Gas is 185kg/h, SO2The rate of recovery of gas is 84%.
Flue gas is with after rich absorbing liquid heat exchange, and temperature is reduced to 90 DEG C by 168 DEG C, and the heat entrained by flue gas is substantially inhaled by richness It receives liquid to absorb, flue gas moisture evaporation amount during spray washing is greatly reduced, and thereby reduces the load of demister, smoke evacuation temperature Degree is reduced to 51 DEG C, and the moisture in flue gas is reduced to 83mg/Nm3, by the air casing added, after flue gas emission " white cigarette " phenomenon is obviously cut down.

Claims (23)

1. a kind of flue gas desulfurization regenerates integrated tower, it is characterised in that：From top to bottom it is followed successively by flue gas emission area, mist eliminating zone, two level Spraying zone holds liquid bath area, level-one spraying zone and regeneration of absorption solution area；The regeneration of absorption solution area by vertical partition board I, every Plate II and partition board III is divided into preheating zone, stripping zone and liquid collecting zone successively by left-to-right, connects with level-one spraying zone at the top of preheating zone Logical, partition board I bottom openings make preheating zone be connected to stripping zone, and the height of partition board II is less than the height of partition board I, stripping zone and liquid collecting Area is connected to by the space on the tops partition board II, by partition board III by stripping zone and liquid collecting zone and spray at the top of stripping zone and liquid collecting zone It is completely separated to drench area；Set of heat exchange tubes is arranged in the preheating zone, and bottom of tower and the flue gas of preheating zone are fixed in the lower end of set of heat exchange tubes Pipeline is connected to, and the upper outlet end of set of heat exchange tubes leads to preheating zone ullage；The set of heat exchange tubes upper outlet end it is upper Side's setting umbrella crown shape baffle；The flue gas emission area is the chimney structure of routine, the chimney bottom and mist eliminating zone tower body It is connected；Outer sleeve is set in chimney top, the outer sleeve is the tubular structure of upper and lower opening, and outer sleeve upper edge is higher by chimney Top certain distance, the lower edge of outer sleeve are less than the upper edge of chimney, are annular space between the outer sleeve and chimney.
2. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The outer sleeve outer sleeve upper edge It is higher by 0.2~10m of chimney top, the lower edge of outer sleeve is less than 0.5 ~ 5m of chimney upper edge；It opens the bottom of the outer sleeve 1.01~1.2 times of a diameter of chimney top opening diameter of mouth.
3. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The both ends the partition board III difference It is connect with partition board I and stripping zone liquid collecting zone tower wall, partition board I and the angle of the junctions partition board III are 45 ~ 165 °；The partition board I, it is sealed between partition board II and partition board III and tower wall, avoids the air-liquid short circuit of partition board both sides.
4. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The partition board I bottom openings face Product is the 2% ~ 30% of partition board I areas, and absorbing liquid enters stripping zone by bottom opening from preheating zone；The partition board II height is The 30% ~ 80% of partition board I height, absorbing liquid enter liquid collecting zone by partition board II upper spaces from stripping zone.
5. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The flue gas emission area and demisting Area is connected by cone-shaped reducing, and the tower diameter ratio in mist eliminating zone and flue gas emission area is 1.5 ~ 5；The mist eliminating zone is sprayed with two level Area is connected by reverse taper deformation diameter, and the tower diameter ratio of mist eliminating zone and two level spraying zone is 1.2 ~ 3；The level-one spraying zone and suction It receives liquid renewing zone by cone-shaped reducing to be connected, the tower diameter ratio of regeneration of absorption solution area and level-one spraying zone is 1 ~ 3.
6. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：Demister is arranged in the mist eliminating zone （12）, demister（12）Including riser I（12-4）, riser II（12-2）And straight tube（12-9）, riser I（12-4）With Riser II（ 12-2）Pass through bearing（12-3）Connection, straight tube（12-9）It is arranged in riser I（12-4）With riser II （12-2）Outside, and with riser I（12-4）,II （12-2）On the same axis；Riser II（12-2）It is fixed on tower Disk（12-1）On；Riser I（12-4）Top setting capping plate（12-7）, several seams are provided in the circumference of riser I （12-5）, stitched close to each item（12-5）Riser I（12-4）It is provided circumferentially about to have tangential flow guiding plate（12-6）, tangentially lead Several cylindrical protrusions are set in flowing plate（10）, straight tube（12-9）Inner wall on be arranged protrusion（12-8）.
7. flue gas desulfurization regenerates integrated tower according to claim 6, it is characterised in that：Protrusion（12-8）To be threaded knot The cylindrical protrusions of structure, cylindrical protrusions（12-8）It is uniformly distributed on deflector, cylindrical protrusions（12-8）Occupied area is The 10% ~ 50% of tangential flow guiding plate 12-6 areas.
8. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The two level spraying zone setting one Layer or Multi-layer sprinkling pipeline, when Multi-layer sprinkling pipeline is arranged, the distance between spray pipe is 0.5 ~ 5m；The spray pipe Lye pipeline I is connected, multiple atomizers are provided on spray pipe；The two level spraying zone is for lye to be atomized, mist Droplet after change is contacted with flue gas adverse current, removes the sulfur dioxide carried in flue gas.
9. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：It is described that hold the setting of liquid bath area several Inflator is risen, flue gas enters two level spraying zone from level-one spraying zone by a liter inflator；Described holds liquid bath area setting one or more Overflow pipe, overflow pipe height enter level-one spraying zone less than inflator height, the lye held in liquid bath is risen by overflow pipe.
10. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：Described holds liquid bath area tower wall one Side is separately connected alkaline solution line I, fresh water pipeline；Flow control valve is set on the alkaline solution line I, for It holds filling alkaline solution in liquid bath and adjusts its pH value；Regulating valve is set on the fresh water pipeline, for holding in liquid bath plus It notes fresh water and adjusts liquid collecting zone liquid level；The liquid bath area bottom of holding is connected with lye extraction pipeline.
11. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The level-one spraying zone setting At least two layers of spray pipe, the distance between spray pipe are 0.5 ~ 5m；The spray pipe connects poor absorbing liquid pipeline I, Multiple atomizers are provided on spray pipe；The level-one spraying zone is for poor absorbing liquid to be atomized, the small liquid after atomization Drop is contacted with flue gas adverse current, removes the sulfur dioxide carried in flue gas.
12. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The set of heat exchange tubes is by least A piece set of heat exchange tubes is at heat exchanger tube is light pipe, fins pipe, screwed pipe, bellows, band pipe, shaped telescopic tube, spiral grooved tube or high pass One or more of buret；The quantity of the heat exchanger tube setting is adjusted according to flue gas flow and smoke inlet temperature It is whole；The set of heat exchange tubes is immersed under the richness absorbing liquid liquid level of preheating zone, the temperature of the rich absorbing liquid after heat exchanger tube exchanges heat It is 60 ~ 95 DEG C.
13. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：Heat exchanger tube cross-sectional area sum is 1 ~ 2 times of flue gas pipeline cross-sectional area.
14. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The stripping zone lower part setting There are stripped vapor distributor pipe, the lower end of stripped vapor distributor pipe to be fixed on the bottom of tower of stripping zone；The stripped vapor distributor pipe It is connected to steam pipe line, several nozzles vertically upward is provided on stripped vapor distributor pipe；The stripping zone uses stripping Steam is as heat medium, and rich absorbing liquid is in the heated regeneration gas decomposited based on sulfur dioxide and steam in stripping zone, shape At poor absorbing liquid.
15. flue gas desulfurization described in accordance with the claim 1 regenerates integrated tower, it is characterised in that：The liquid collecting zone tower wall side Connect alkaline solution line II, outer comb line and liquid level gauge；The liquid collecting zone is used to collect the poor absorbing liquid after regeneration；It is described Alkaline solution line II on flow control valve is set, for into poor absorbing liquid fill alkaline solution adjust its pH value；It is described Outer comb line for that will be arranged outside a small amount of poor absorbing liquid to reduce the sulfate concentration in poor absorbing liquid；Above the liquid collecting zone Gas vent is arranged in tower wall, for connecting regeneration gas pipeline；The liquid collecting zone bottom is connected with poor absorbing liquid pipeline II, uses In connection bottom of tower circulating pump.
16. a kind of Regeneratable wet fuel gas desulfurizing technology, it is characterised in that：The claims 1 ~ 15 are used in the technique The flue gas desulfurization of one claim regenerates integrated tower.
17. Regeneratable wet fuel gas desulfurizing technology according to claim 16, it is characterised in that including the following contents：Dedusting The preheating zone bottom that flue gas afterwards regenerates integrated tower through flue gas pipeline from flue gas desulfurization enters set of heat exchange tubes, is inhaled with the richness of preheating zone Enter level-one spraying zone above set of heat exchange tubes after receiving liquid heat exchange, flue gas and the poor absorbing liquid counter current contacting of level-one spraying zone remove Most of sulfur dioxide, enters two level spraying zone across the flue gas of level-one spraying zone in flue gas, inverse in two level spraying zone and lye Stream contact carries out deep desulfuration, and purified flue gas enters outer sleeve from the chimney top in flue gas emission area and is sufficiently mixed with air Afterwards from flue gas emission area top discharge；With the rich absorbing liquid after flue gas heat exchange below the partition board I between preheating zone and stripping zone Into stripping zone, it is heated by steam the regeneration gas decomposited based on sulfur dioxide and steam, forms poor absorbing liquid；Poor absorption Liquid enters liquid collecting zone under the impetus of steam, is arranged outside a small amount of poor absorbing liquid, and remaining poor absorbing liquid is taken out from the bottom of liquid collecting zone Go out, level-one spraying zone is entered after cooling and is recycled, gas vent discharge of the regeneration gas through stripping zone top.
18. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：The flue gas is fire coal Boiler smoke, coal-fired plant flue gas, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, coking flue gas or steel are burnt Tie one or more of flue gas.
19. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：The alkaline solution is In sodium hydroxide solution, potassium hydroxide solution, sodium carbonate liquor, solution of potassium carbonate, sodium sulfite solution or potassium sulfite solution One or more.
20. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：The poor absorption liquid pH Value control is 6.0 ~ 7.5, and the pH value of poor absorbing liquid is controlled by controlling the alkaline solution flow into liquid collecting zone.
21. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：It is absorbed in two level spraying zone The lye of sulfur dioxide is extracted out from holding liquid bath bottom after being mixed with fresh water, fresh lye, is followed after the pressurization of stage casing circulating pump Ring uses；The lye pH value control is 5.0 ~ 7.5.
22. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：The rich absorbing liquid with Temperature after flue gas heat exchange is 60 ~ 95 DEG C, and rich absorbing liquid enters stripping zone, and the temperature after being heated by steam is 70 ~ 100 DEG C.
23. Regeneratable wet fuel gas desulfurizing technology according to claim 17, it is characterised in that：The stripping zone pressure In -200 ~ 200kPa, the pressure is gauge pressure for control, stripping zone pressure by air-introduced machine inlet vane aperture or air-introduced machine frequency conversion Motor is controlled.
CN201710299537.6A 2017-05-02 2017-05-02 Flue gas desulfurization and regeneration integrated tower and renewable wet flue gas desulfurization method Active CN108786398B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201710299537.6A CN108786398B (en) 2017-05-02 2017-05-02 Flue gas desulfurization and regeneration integrated tower and renewable wet flue gas desulfurization method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201710299537.6A CN108786398B (en) 2017-05-02 2017-05-02 Flue gas desulfurization and regeneration integrated tower and renewable wet flue gas desulfurization method

Publications (2)

Publication Number Publication Date
CN108786398A true CN108786398A (en) 2018-11-13
CN108786398B CN108786398B (en) 2020-12-08

Family

ID=64053464

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201710299537.6A Active CN108786398B (en) 2017-05-02 2017-05-02 Flue gas desulfurization and regeneration integrated tower and renewable wet flue gas desulfurization method

Country Status (1)

Country Link
CN (1) CN108786398B (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110433645A (en) * 2019-09-09 2019-11-12 中船动力研究院有限公司 A kind of flue gas desulfurization device
CN112403214A (en) * 2020-10-30 2021-02-26 攀枝花市蓝鼎环保科技有限公司 Novel flue gas desulfurization tower
CN112717673A (en) * 2020-11-28 2021-04-30 安徽金禾实业股份有限公司 Desulfurization method for analytic waste gas in desulfurization liquid regeneration tank
CN115011382A (en) * 2022-07-18 2022-09-06 中国科学院过程工程研究所 Blast furnace gas desulfurization and regeneration integrated tower and application thereof
WO2023118860A1 (en) * 2021-12-22 2023-06-29 Edwards Limited Mist trap

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101185838A (en) * 2007-08-24 2008-05-28 中国石油化工集团公司 Regeneratable wet fuel gas desulfurizing technology
CN101433804A (en) * 2008-12-02 2009-05-20 中冶焦耐工程技术有限公司 Gas recirculation type technique and device for regenerating doctor for wet oxidation process
CN103252161A (en) * 2013-05-11 2013-08-21 山东中玻节能环保发展有限公司 Renewable organic amine circulation desulfurization purification tower and renewable organic amine circulation desulfurization technology
CN103877831A (en) * 2014-04-03 2014-06-25 江汉大学 Integrated complex ferrous wet flue gas desulfurization and denitration method
CN104624029A (en) * 2015-01-06 2015-05-20 山东大学 Device for integrating cooling tower, desulfurizing tower and chimney, and desulfurizing method
US20150139881A1 (en) * 2013-11-21 2015-05-21 Mitsubishi Heavy Industries, Ltd. Wet type flue-gas desulfuization apparatus and method for adjusting oxidation reduction potential of absorbent therefor
CN106178896A (en) * 2016-08-26 2016-12-07 江苏中圣高科技产业有限公司 The desulfurizer of a kind of ammonia circulation utilization and method
CN106310943A (en) * 2016-08-31 2017-01-11 上海交通大学 Device for regenerating sodium sulfite desulphurization liquid and recycling sulfur dioxide with sodium sulfite desulphurization liquid and application of device
CN205974440U (en) * 2016-08-30 2017-02-22 高翔 Two circulation process devices of a coal gas desulfurization tower

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101185838A (en) * 2007-08-24 2008-05-28 中国石油化工集团公司 Regeneratable wet fuel gas desulfurizing technology
CN101433804A (en) * 2008-12-02 2009-05-20 中冶焦耐工程技术有限公司 Gas recirculation type technique and device for regenerating doctor for wet oxidation process
CN103252161A (en) * 2013-05-11 2013-08-21 山东中玻节能环保发展有限公司 Renewable organic amine circulation desulfurization purification tower and renewable organic amine circulation desulfurization technology
US20150139881A1 (en) * 2013-11-21 2015-05-21 Mitsubishi Heavy Industries, Ltd. Wet type flue-gas desulfuization apparatus and method for adjusting oxidation reduction potential of absorbent therefor
CN103877831A (en) * 2014-04-03 2014-06-25 江汉大学 Integrated complex ferrous wet flue gas desulfurization and denitration method
CN104624029A (en) * 2015-01-06 2015-05-20 山东大学 Device for integrating cooling tower, desulfurizing tower and chimney, and desulfurizing method
CN106178896A (en) * 2016-08-26 2016-12-07 江苏中圣高科技产业有限公司 The desulfurizer of a kind of ammonia circulation utilization and method
CN205974440U (en) * 2016-08-30 2017-02-22 高翔 Two circulation process devices of a coal gas desulfurization tower
CN106310943A (en) * 2016-08-31 2017-01-11 上海交通大学 Device for regenerating sodium sulfite desulphurization liquid and recycling sulfur dioxide with sodium sulfite desulphurization liquid and application of device

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110433645A (en) * 2019-09-09 2019-11-12 中船动力研究院有限公司 A kind of flue gas desulfurization device
CN112403214A (en) * 2020-10-30 2021-02-26 攀枝花市蓝鼎环保科技有限公司 Novel flue gas desulfurization tower
CN112717673A (en) * 2020-11-28 2021-04-30 安徽金禾实业股份有限公司 Desulfurization method for analytic waste gas in desulfurization liquid regeneration tank
WO2023118860A1 (en) * 2021-12-22 2023-06-29 Edwards Limited Mist trap
CN115011382A (en) * 2022-07-18 2022-09-06 中国科学院过程工程研究所 Blast furnace gas desulfurization and regeneration integrated tower and application thereof

Also Published As

Publication number Publication date
CN108786398B (en) 2020-12-08

Similar Documents

Publication Publication Date Title
CN105854561B (en) The device and technique that a kind of flue gas desulfurization, dedusting collaboration are administered
CN100525885C (en) Turbine type pressure charging acceleration fuel gas desulfurization gas wash tower
CN108786398A (en) Flue gas desulfurization regenerates integrated tower and Regeneratable wet fuel gas desulfurizing method
CN110559804B (en) Flue gas desulfurization and regeneration integrated tower and flue gas desulfurization method
CN103868087B (en) A kind of collaborative enhancing PM2.5The method of elimination and fume afterheat deep exploitation and device
CN106693657B (en) A kind of single column double circulation desulphurization and dust-removing device and technique
CN108686490A (en) A kind of fuel gas desulfurization gas wash tower and desulfurization and dust-removal method
CN108619872A (en) A kind of fume desulfurizing tower and flue gas desulfurization and wastewater treatment method
CN205886590U (en) Gas wash tower and SOx/NOx control system
CN208990512U (en) A kind of flue gas of wet desulphurization disappears white system
CN107398166A (en) A kind of water-saving smoke-gas wet desulfurization spray column
CN203002194U (en) Turbulent ball turbocharged composite desulphurization dedusting tower
CN108686492B (en) Flue gas dust removal desulfurization tower and dust removal desulfurization method
CN108619885A (en) A kind of fume desulfurizing tower and flue gas ash removal, desulfurization and wastewater treatment method
CN209108927U (en) A kind of industrial waste gas processing system
CN101143298B (en) High-efficiency wet-desulfurizing dust remover
CN108686493B (en) Flue gas dust removal desulfurization tower and dust removal desulfurization process
CN2843595Y (en) Multi-stage spiral-plate leaf desulfurizing dust collector
CN105396451B (en) Caustic dip efficient removal SO in a kind of spray desulfurizing tower3Technique
CN205903744U (en) Administer bagasse exhaust gas of boiler's dehydration gas wash tower
CN205850573U (en) A kind of SO2minimum discharge micro-alternating temperature energy-saving and smoke-removing system
CN108786427A (en) Flue gas desulfurization regenerates integrated tower and Regeneratable wet fuel gas desulfurizing technology
CN1221307C (en) Integrative desulfurizing and dedusting tower of ammonia process
CN207169353U (en) Composite boiler flue-gas dust-removing and desulfurization device
CN208626955U (en) Flue gas washing system

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right

Effective date of registration: 20230829

Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee after: CHINA PETROLEUM & CHEMICAL Corp.

Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd.

Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee before: CHINA PETROLEUM & CHEMICAL Corp.

Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp.

TR01 Transfer of patent right