CN104607018B - H-shaped flue gas dust removal desulfurization reactor and flue gas desulfurization method - Google Patents
H-shaped flue gas dust removal desulfurization reactor and flue gas desulfurization method Download PDFInfo
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Abstract
The present invention discloses an H-shaped flue gas dust removal desulfurization reactor and a flue gas desulfurization method. The reactor of the present invention comprises a pre-treatment unit and a deep treatment unit, wherein the two units form an H-shaped double-tower structure, the pre-treatment unit sequentially comprises a flue gas inlet, a turbulent scrubber, a common jujube seed-shaped regular packing assembly and a first-stage liquid holding tank from top to bottom, the deep treatment unit comprises a second-stage liquid holding tank, a packing assembly, a demister assembly and a purified flue gas outlet from bottom to top, and the pre-treatment unit and the deep treatment unit are communicated through the flue gas channel on the middle portion. The reactor of the present invention can achieve functions of one spraying and two-stage absorption/purification, has advantages of high contaminant removal rate, low energy consumption and the like, and is especially suitable for the dust removal desulfurization process of high dust content flue gas.
Description
Technical field
The invention discloses a kind of H type flue-gas dust-removing and desulfurization reactor and fume desulphurization method, belong to field of environment protection, it is adaptable to flue gas and process tail gas dust-removal and desulfurizing process, and can be widely applied to the field such as petrochemical industry and environmental protection.
Background technology
In the atmospheric pollution of China, acid rain and floating dust are topmost pollutions.During the last ten years, owing to the discharge capacity of sulfur dioxide and nitrogen oxides day by day increases, the problem of acid rain is more and more prominent.China has been the third-largest Acid Rain Zone being only second to Europe and North America now.SO2It is the major reason causing China's atmospheric pollution with dust, the atmosphere pollution of the current priority control of Ye Shi China.China SO2Total emission volumn is the most for years more than 20,000,000 tons, within 2005, total emission volumn reaches 25,490,000 tons, occupying first place in the world, although the target that China the Eleventh Five-Year Plan period cuts down sulfur dioxide 10% has been carried out, but the Acid Rain Pollution area that China is current (accounting for the 30% of area) is still constantly expanding.Annual because of acid rain and SO2Polluting and cause the economic loss of the aspects such as crops, forest and health more than 100,000,000,000 yuan, sulfur dioxide (SO2) emissions control still to can not be ignored.Dust refers to particle diameter 1～the particulate matter of 75 microns.Typically produced by broken in commercial production, runs.According to analysis, China is entered the dust of air every year by industry and life cellar for storing things fire grate, more than 10,000,000 tons.Dust is easily inhaled into human respiratory tract's system, directly threatens the life of people, and the environment being especially in dust pollution can cause multiple cardiovascular, respiratory tract disease etc..
Flue gas desulfurization is pressed the kind of desulfurizing agent and is divided, and can be divided into following five kinds of methods: with CaCO3Calcium method based on (limestone), the magnesium processes based on MgO, with Na2SO3Based on sodium method, with NH3Based on ammonia process, the organic alkaline process based on organic base.Presently, it is recognized that desulfurization dust-removing technique include water film type, fountain, impact type and water-bath type etc..Venturi and rapid punching are as strengthening gas-liquid mass transfer (contact) equipment, flue-gas dust-removing and desulfurization device is widely used, wherein venturi height about 16m～19m, and when exhaust gas volumn is bigger, whole desulfurizer is that multiple venturi encircles form with desulfurizing tower, take up room and invest the biggest, such as the flue gas desulfurization technique of Norton.Rapid punching needs liquid phase is raised 6～8m, to produce froth zone, and by the continuous renewal of foam, keeps efficient gas-liquid mass transfer effect, but the most therefore the height of reactor and infrastructure investment substantially increase.
Patent US3894563A and patent US2012000366A1 all use venturi to realize dedusting and gas-liquid separation with cyclone separator combination.In desulfurizer that patent CN200920247553.1, CN200920200026.5 and CN03142049.4 introduce or technique, rapids rushes scrubbing tower and is and is separately provided, and floor space is big, and investment cost is high.
Patent US4110088 describes the cooling of a kind of high-temperature flue gas chilling, dedusting and the technique of removing water soluble contaminants and device.The high-temperature flue gas of 927～1038 DEG C is after two-stage spraying cooling, enter cyclone separator and isolate drop and dust, carry out removing pollutant in waste gas through packed tower again, after the deflection plate demister of purification gas entrance band fin plate is except mist, finally being injected into aiutage through venturi, purification gas, when venturi ejection at a high speed, produces negative pressure, suction venturi surrounding air, makes purification gas humidity reduce.This technological process is long, and pressure drop is very big, is provided with twice blower fan in technique, and with thinking that flue gas provides power, energy consumption is bigger.
CN101301574A discloses a kind of multi-stage flue gas desulfurization spray column, and including primary desulfurizing scrubber and secondary desulfuration spray tower, the outlet of described primary desulfurizing scrubber is connected with the entrance of secondary desulfuration spray tower.This multi-stage flue gas desulfurization tower also includes return duct, this connecting tube is connected between the bottom of primary desulfurizing scrubber and secondary desulfuration spray tower, thus, absorbing liquid is back to secondary desulfuration spray tower through this return duct, is equivalent to one circulatory pool of two-step desulfurization units shared.What this technology realized has the technical effect that once desulfurization in primary desulfurizing scrubber, secondary desulfuration in secondary desulfuration spray tower, this one circulatory pool of technology two-step desulfurization units shared, it is formed without the grating region of absorbing liquid, desulfurization degree is the highest, and this absorption of technology agent uses lime stone slurry, and the return duct between two-step desulfurization unit is only by gravity reflux, therefore reflux pipeline is easy to blocking, this Chief Technology Officer period run reliability is not enough.
CN2608111Y discloses a kind of high-concentration fume desulfurating dust-removing equipment, this technology is overlapped above desulfurization unit 2 and is cascaded, with a shell, the desulfurization unit of series connection is covered on together, bottom shares a circulating slot, this technology circulatory pool does not has to process for the feature of high-concentration fume, is only cascaded by the two above desulfurization units of set, and desulfuration efficiency ensure that, but take up an area relatively big, be not suitable for the reserved less region in place and use.
In prior art, though the cooling/dedusting of high-temperature flue gas/desulfurization uses two-stage or multi-stage gas-liquid contact absorption technique, having reached pollutant removing effect, but every one-level spray-absorption is provided with corresponding equipment for liquid transportation and absorbing liquid atomization plant, energy consumption is higher.
Summary of the invention
For existing Venturi scrubber and the deficiency of turbulent impulse scrubber fume treatment technology, the invention provides a kind of H type flue-gas dust-removing and desulfurization reactor and fume desulphurization method, the high potential energy and the date core shaped structured packing that utilize turbulent impulse scrubber absorbing liquid carry out pretreatment to flue gas simultaneously, and wherein turbulent impulse scrubber is positioned at the top of date core shaped structured packing.Turbulent impulse scrubber absorbing liquid is during declining, because of the wind-force dissection by pretreatment unit flue gas, it is dispersed into tiny drop/droplet, when gas-liquid two-phase is also cross date core shaped structured packing, there is strengthening effect of mass transmitting at this between gas-liquid two-phase, it is achieved thereby that once spray, twice strengthening mass transfer absorbs, and equipment for liquid transportation effect is fully used to the energy of turbulent impulse scrubber absorbing liquid.
The invention provides a kind of H type flue-gas dust-removing and desulfurization reactor, it is characterised in that described reactor includes pretreatment unit and advanced treatment unit, the two constitutes " H " shape or " u "-shaped Double-Tower Structure；Wherein said pretreatment unit includes that smoke inlet, moisture film assembly, turbulent impulse scrubber, date core shaped structured packing assembly I and one-level hold liquid bath from top to bottom, and described advanced treatment unit includes that two grades are held liquid bath, filler assembly, demister and purifying smoke outlet from bottom to top；Described pretreatment unit is connected by the exhaust gases passes at middle part with advanced treatment unit.
H type flue-gas dust-removing and desulfurization reactor according to the present invention, wherein said pretreatment unit also includes primary cycle pump and primary cycle pipeline；Equally, described advanced treatment unit also includes secondary cycle pump, secondary cycle pipeline and two grades of spray systems.Two grades of described spray systems are positioned at above or below filler.
H type flue-gas dust-removing and desulfurization reactor according to the present invention, wherein in described pretreatment unit, on the top of wall of reactor, preferred reactor wall arranges moisture film assembly with the connecting portion of smoke inlet reducing.Described moisture film assembly can use the structure of any suitable form in this area, as arranged endless tube in wall of reactor surrounding, endless tube arranges the nozzle towards tower wall.And in the present invention, it is preferred to overflow-type moisture film assembly is set at the connecting portion of wall of reactor Yu smoke inlet reducing.The structure of described overflow-type moisture film assembly is: the lower end of smoke inlet reducing connects one section of straight tube, the diameter of this direct tube section is more than the reactor diameter of pretreatment unit, connecting portion at wall of reactor and reducing forms the cannelure that a bottom lock, upper end are uncovered, preferably at the uncovered employing tooth-shape structure of cannelure.This cannelure is held liquid bath with one-level and is connected by pipeline.When liquid constantly injects in annular space, liquid constantly can flow down along the inwall of cylinder along the upper edge of cylinder with overflow type, from top to bottom, thus covers whole wall of reactor.Owing to doing/wet interface at reactor inlet; heat smoke touches shower water for the first time; the acid mist of high concentration can be produced; so the corrosion condition at dry/wet interface is extremely serious, by using the form of moisture film protection, it is possible to reduce the corrosion condition at dry/wet interface; and the fouling that will be attached on reactor wall rinses at any time; avoid underdeposit corrosion, improve the antiseptic power of material or reduce the consumption of high anticorrosion material, thus significantly reducing cost.
H type flue-gas dust-removing and desulfurization reactor according to the present invention, wherein, described turbulent impulse scrubber is made up of nozzle and pipeline.
H type flue-gas dust-removing and desulfurization reactor according to the present invention, described date core shaped structured packing assembly, including date core shaped structured packing I, it includes the packing layer that more than at least one of which, preferred two-layer are made up of some parallel connections, horizontal positioned date core shaped special pipe, and described some parallel connections, the date core shaped special pipe of horizontal positioned constitute multiple has collection section, aditus laryngis and the parallel channels of dispersion section.Date core shaped structured packing can be made into one or is divided into some pieces of block combiner to use.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, the cross section (i.e. end face) of described date core shaped special pipe is date core shaped, and its top and bottom are acute triangle, and middle part is circular arc, forms the date core shaped of " Rhizoma Anemones Raddeanae middle circle ".The middle part of date core shaped special pipe is arc surface, and the dust being beneficial to contain in gas is under hygrometric state, under the brushing of self gravitation and gas phase, by the downward landing of this slip flow regime, thus avoids channel blockage phenomenon.
Two end faces of described date core shaped special pipe can be closed or do not close.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, preferably arranging some parallel, boss of protuberance on the both sides tube wall of date core shaped special pipe, described boss preferably has certain inclination angle.The cross section of described boss can be the suitable shapes such as circular, triangle or rectangle, circular.The boss that special pipe both sides tube wall is arranged, can symmetrical or mal-distribution.And the upper end starting point of groove is preferably lower than the phase tangent line of downside tube wall and the circular arc tube wall on both sides.
A rule crack is formed between boss and tube wall that both sides, date core shaped special pipe bottom tube wall is arranged, after being conducive to wall flow liquid drip to go out aditus laryngis, blow lower drop in gas phase and blown entrance crack, and in crack, realize coalescence, such that it is able to elimination entrainment, it is simple to realize gas-liquid separation.
Along zigzag can also be arranged under date core shaped special pipe, it is beneficial to after wall flow liquid drip goes out special pipe, form equally distributed continuous stream.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, described date core shaped special pipe structured packing is defined by some special pipes in parallel has collection section, aditus laryngis and the passage of dispersion section.When the flue gas after turbulent impulse scrubber spray-absorption and absorbing liquid and flow this packing area of entrance, initially enter collection section (aisle spare contraction), gas velocity increases, realizing solution dispersion, liquid phase specific surface area increases, and the grit attachment being captured not yet is moistening, scattered atomic drop is under the contention effect of high-speed gas, due to the ductility of water, will attach to be formed on tube wall liquid film, it is achieved that the coalescence of drop and samming process.When liquid film is by aditus laryngis, due to the further increase of gas velocity, liquid film creating again strong compressing and dissection, liquid film is the most thinning, creates twice dispersing effect；After aditus laryngis, gas velocity declines rapidly, in the process, the a large amount of dust contained in gas are due to the change of gas velocity, realizing mud and drip coalescence, dust along interface landing, thus will realize dedusting function, and liquid film is on the tube wall of two side lower parts of date core shaped special pipe during flow down, clamp-oned in the boss crack with tube wall by gas again, it is achieved that coalescence again, and finally become continuous wire to be dripped by the bottom of date core shaped special pipe, thus eliminate entrainment, complete mass transfer reaction.
Owing to employing date core shaped structured packing, the H type flue-gas dust-removing and desulfurization reactor of the present invention is particularly well-suited in flue gas the operating mode bigger containing Dust Capacity.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, random packing or the structured packing assemblies such as rectangular saddle ring, Pall ring, Raschig ring are typically selected in the packing area of advanced treatment unit.Present invention preferably employs is date core shaped structured packing, and its structure is identical with the structure of the date core shaped structured packing assembly used by pretreatment unit, and it is not both this filler assembly preferably only with one layer of date core shaped structured packing.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, two grades of described spray systems are positioned at above or below filler assembly, and flue gas countercurrently or and flows contact mass transfer with spray liquid.Spray liquid, under flue gas upwards blows, will produce the froth bed of the turbulence of certain altitude above filler assembly, and at this moment gas-liquid two-phase not only contact surface is big, and contact surface alkali liquor is continuously available renewal, gas-liquid two-phase fierceness collisional mixing, reaches efficient mass transfer reaction, it is achieved mass transport process.And liquid phase falls into two grades in the effect of self gravitation holds in liquid bath.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, described demister can use the demister of routine, as used broken line type or streamlined demister.In the present invention, described demister preferred deflector type demister, it includes that several are arranged side by side except mist assembly, each all includes riser and urceolus except mist assembly, and urceolus is arranged on the outside of riser, and with riser on the same axis；Riser is fixed on tower tray, and the top of riser arranges capping plate, and the circumference at riser has some seams, provided circumferentially about has the tangential flow guiding wing at the riser near each bar seam.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, the urceolus of wherein said demister is made up of direct tube section and conical cylinder section.The inner surface (inwall) of urceolus can also arrange projection, and heretofore described projection preferably employs the clapper structure that cross section is rectangle.Wherein, the direction of rotation of hyoplastron is preferably contrary with the direction of rotation of the tangential flow guiding wing.In the deflector type demister of the present invention, the lower ending opening of described urceolus can also be arranged to zigzag structure, thus advantageously becomes continuous drip to fall in isolated liquid from the inwall of urceolus.
In the H type flue-gas dust-removing and desulfurization reactor of the present invention, described deflector type demister realizes the high efficiency separation of drop and gas by the fluid repeatedly baffling in flow process.
The present invention can also place floating basket in the one-level of pretreatment unit holds liquid bath, places oxidation catalyst such as iron ore in floating basket.Holding absorbing liquid in liquid bath due to one-level is faintly acid, and iron ore can be dissolved and be converted into manganese ion or the iron ion with catalysis.Containing manganese ion or iron ion first order absorption liquid by primary cycle transport pump to turbulent impulse scrubber, its spray liquid contacts with flue gas adverse current, in flue gas oxygen is transferred in liquid phase.First order absorption liquid and the SO in flue gas2Reaction generates sulphite or bisulfites, afterwards dissolved oxygen and there is catalysis manganese ion or iron ion action under, the oxidized sulfate that is converted into, thus reduce the COD in waste water, make discharged wastewater met the national standard.
Another technical problem to be solved by this invention is to provide a kind of process for dusting and dsulfurizing fume, the method uses H type flue-gas dust-removing and desulfurization reactor recited above.
A kind of process for dusting and dsulfurizing fume of the present invention, specifically includes herein below:
(1) high-temperature flue gas is after over-quenching is lowered the temperature, enter pretreatment unit, it is neutral or acid first order absorption liquid counter current contacting with the pH value of turbulent impulse scrubber ejection, rapids rushes absorbing liquid during declining, it is dispersed into tiny drop/droplet by the wind-force dissection of gas in tower, carries out in this process lowering the temperature, dedusting and pre-desulfurization；
(2) flue gas after step (1) first order absorption continues with absorbing liquid and stream flows downward, and enters date core shaped structured packing assembly, and completes further at this absorbing the cooling of flue gas, dedusting and pre-desulfurization；
(3) the first order absorption liquid entrance one-level absorbing sulfur dioxide holds liquid bath, and is recycled by primary cycle pump and primary cycle pipeline；
(4) flue gas after pretreatment unit absorbs is under the promotion of upper pressure, advanced treatment unit is entered by the passage between pretreatment unit and advanced treatment unit, and upwardly through filler assembly, and with filler assembly below or above spray system injection pH value in alkalescence two grades of absorbing liquids be fully contacted mass transfer at filler assembly, complete final sweetening process；
(5) by flue gas after the purification of filler assembly by except mist assembly, after gas-liquid separation, discharge from dust-removal and desulfurizing reactor exhanst gas outlet.
In the process for dusting and dsulfurizing fume of the present invention, it is respectively provided with at pretreatment unit and advanced treatment unit and holds liquid bath, define independent Two-way Cycle flue-gas dust-removing and desulfurization system.Holding for two and arrange passage in the middle of liquid bath, one-level is held liquid bath and is provided absorbing liquid for pretreatment unit, holds liquid bath for two grades and provides absorbing liquid for advanced treatment unit.This technique proposes desulfurization absorbing liquid concentration grating theory, and original absorbance liquid initially enters two grades and holds liquid bath, then holds liquid bath by center-aisle entrance one-level, and it is final absorbing liquid discharge pond that one-level holds liquid bath.For guaranteeing the utilization rate of absorbing liquid, the pH value holding liquid bath by controlling one-level controls to enter two grades of alkali liquor amounts holding liquid bath, owing to this technological process is able to ensure that two grades of pH value holding liquid bath are alkalescence, thus can be greatly improved desulfurization degree.Hold the pH value of liquid bath by controlling I and II, both ensure that the high efficiency of this fume desulphurization method, and may insure that again the utilization rate that desulfurization absorbing liquid is higher.
In the process for dusting and dsulfurizing fume of the present invention, flue gas can be from the sulfur-bearing dust-laden high-temperature flue gas in various devices, the wherein SO of flue gas2Concentration is 500～5000mg/Nm3, preferably 1000～4000mg/Nm3；Dust concentration 200～800mg/Nm3, preferably 300～500mg/Nm3。
In the process for dusting and dsulfurizing fume of the present invention, the operating condition of reactor is: operation temperature is 100～350 DEG C, preferably 150～200 DEG C；Operation pressure is normal pressure to 1MPa；Treatment quantity is 500～200000m3/ h, preferably 700～190000m3/h；Absorbing liquid circulating load is 0.4m3/ h～7m3/ h, preferably 0.5m3/ h～6m3/h。
In the process for dusting and dsulfurizing fume of the present invention, described absorbing liquid can be NaOH solution, Na2CO3Solution, Mg (OH)2Solution or lime water Ca (OH)2, the preferred NaOH solution of absorbing liquid of this technique employing, the pH value of the first order absorption liquid during wherein one-level holds liquid bath is between 6～7, and two grades of absorbing liquid pH value that described two grades are held in liquid bath are between 8～10.
Compared with prior art, flue-gas dust-removing and desulfurization reactor and the process for dusting and dsulfurizing fume of the present invention has the advantage that
1, the cooling of flue gas chilling and dust-removal and desulfurizing treatment effect are strengthened greatly.Rapids rushes absorbing liquid during declining, and is dispersed into tiny drop/droplet by the wind-force dissection of gas in tower, and in date core shaped structured packing, the effect of mass transmitting between gas-liquid two-phase is further strengthened.
2, the present invention can make full use of rapids and rush the high potential energy of absorbing liquid.Invention achieves absorbing liquid once to spray, the effect of twice absorption, compare existing two-stage or multi-stage flue gas treatment technology, save the energy consumption being separately provided venturi slurry circulating pump.
3, the flue-gas dust-removing and desulfurization reactor of the present invention; use moisture film assembly; achieve the protection of the moisture film to pretreatment unit wall of reactor; decrease the equipment corrosion of pretreatment unit; improve the antiseptic power of material or reduce the consumption of high-grade anticorrosion material, thus significantly reducing construction costs.
4, the process for dusting and dsulfurizing fume of the present invention, it is proposed that desulfurization absorbing liquid concentration grating theory.Hold liquid bath by being respectively provided with at pretreatment unit and advanced treatment unit, define independent Two-way Cycle flue-gas dust-removing and desulfurization system.The pH value being held liquid bath by one-level controls to enter two grades of fresh soda liquid measures holding liquid bath, so that it is guaranteed that two grades of pH value holding liquid bath maintain higher basicity, thus substantially increases desulfurization degree.One-level holds liquid bath, the zonal control of two grades of pH value holding liquid bath, both ensure that the high efficiency of this fume desulphurization method, and may insure that again the utilization rate that desulfurization absorbing liquid is higher.
Accompanying drawing explanation
Fig. 1 is flue-gas dust-removing and desulfurization structure of reactor schematic diagram of the present invention.
In Fig. 1: 1-moisture film assembly；2-turbulent impulse scrubber；3-date core shaped structured packing assembly；4-primary cycle pipeline；5-primary cycle pump；6-one-level holds liquid bath；7-bis-grades holds liquid bath；8-passage；9-secondary cycle pump；10-secondary cycle pipeline；11-filler assembly；Bis-grades of spray systems of 12-；13-demister；14-purifying smoke exports；15-smoke inlet；16-urceolus；17-base plate；18-cylinder.
Fig. 2 is the structural representation of the date core shaped structured packing assembly of the present invention.
In Fig. 2: 31-pull bar；32-date core shaped special pipe；33-housing；34-flange, 35-collection section；36-aditus laryngis；37-disperses section；18-cylinder.
Fig. 3 is the structural representation of date core shaped special pipe.
321-boss in figure.
Fig. 4 is the deflector type demister structural representation of demister assembly of the present invention.
In Fig. 4: 131-tower tray；132-riser；133-urceolus；The 134-tangential flow guiding wing；135-covers plate；136-bar stitches；137-groove；138-direct tube section；139-conical cylinder section.
Fig. 5 is the Section A-A top view except mist assembly.
Detailed description of the invention
Technology contents and the effect of the present invention is further illustrated below in conjunction with the accompanying drawings with embodiment.
As shown in Figure 1, the flue-gas dust-removing and desulfurization reactor of the present invention includes pretreatment unit and advanced treatment unit, the two constitutes " H " type Double-Tower Structure, and wherein said pretreatment unit includes that smoke inlet 15, moisture film assembly 1, turbulent impulse scrubber 2, date core shaped structured packing assembly I 3 and one-level hold liquid bath 6 the most successively；Described advanced treatment unit includes that two grades are held liquid bath 7, filler assembly 11, demister assembly 13 and purifying smoke outlet 14 from bottom to top, and pretreatment unit is connected by the exhaust gases passes 8 at middle part with advanced treatment unit.
The flue-gas dust-removing and desulfurization reactor of the present invention, wherein said pretreatment unit also includes primary cycle pump 5 and primary cycle pipeline 4；Described advanced treatment unit also includes secondary cycle pump 9, secondary cycle pipeline 10 and two grades of spray systems 12.Two grades of described spray systems 12 are positioned at the top of filler assembly 11, and certainly, two grades of spray systems 12 can also be positioned at the lower section of filler assembly 11.
In the flue-gas dust-removing and desulfurization reactor of the present invention, described moisture film assembly 1 can use the structure of any suitable form in this area.In Fig. 1, moisture film assembly 1 includes smoke inlet reducing 20, along 19 on the reactor shell 18 of direct tube section 16, base plate 17 and pretreatment unit that lower end connects, defined a cannelure by direct tube section 16, base plate 17 and cylinder along 19, and hold liquid bath 6 by primary cycle pipeline 4, primary cycle pump 5 with one-level and be connected.Wherein the diameter of direct tube section 16 is more than the diameter of cylinder 18.Wherein along the 19(i.e. opening of cannelure on preferred cylinder) it is preferably provided to tooth-shape structure.
The flue-gas dust-removing and desulfurization reactor of the present invention, described turbulent impulse scrubber 2 can be selected for any form of rapids and rushes nozzle.
The flue-gas dust-removing and desulfurization reactor of the present invention, described date core shaped structured packing assembly is connected by pull bar 31 by the date core shaped special pipe 32 of some horizontal positioned in parallel, date core shaped special pipe 32, and is fixed on housing 33.On cylinder 18 inwall, support lugn 34 is set, is used for fixing date core shaped structured packing is installed.Defining a plurality of parallel channels between some parallel date core shaped special pipes 32, constitute gas liquid two-phase flow passage, described passage includes collection section 35, aditus laryngis 36 and dispersion section 37.As it is shown on figure 3, preferably arrange some parallel, boss 321 of protuberance on the tube wall of special pipe.
The flue-gas dust-removing and desulfurization reactor of the present invention, the described demister in demister assembly includes riser 132 and urceolus 133, urceolus 133 is arranged on the outside of riser 132, and with riser 132 on the same axis, urceolus 133 is made up of direct tube section 138 and conical cylinder section 139.Riser 132 is fixed on tower tray 131, and the top of riser arranges capping plate 135, and the circumference at riser has some seams 136, provided circumferentially about has the tangential flow guiding wing 134 at the riser near each bar seam.The inner surface (inwall) of inversed conical drum 133 is further opened with hyoplastron 137.
During work; high-temperature flue gas through over-quenching lower the temperature after by smoke inlet 15; initially enter pretreatment unit; the primary cycle liquid that one-level is held in liquid bath 6 is flowed to moisture film assembly 1 by primary cycle pump 5 part; reactor is formed liquid film protection; another part is transported to turbulent impulse scrubber 2; the first order absorption liquid counter current contacting that high-temperature flue gas sprays with turbulent impulse scrubber 2; rapids rushes absorbing liquid during declining; it is dispersed into tiny drop/droplet by the wind-force dissection of gas in tower, carries out in this process lowering the temperature, dedusting and pre-desulfurization；Flue gas after first order absorption continues with absorbing liquid and stream flows downward, and enters date core shaped structured packing assembly 3, and completes further at this absorbing the cooling of flue gas, dedusting and pre-desulfurization；Absorb the first order absorption liquid of sulfur dioxide to fall into one-level and hold liquid bath 6, and recycled by primary cycle pump 5 and primary cycle pipeline 4；And the flue gas after pretreatment unit absorption is under the promotion of upper pressure, enter advanced treatment unit by the passage 8 between pretreatment unit and advanced treatment unit.Flue gas after first order absorption is upwardly through filler assembly 11, and it is fully contacted mass transfer with the two grades of absorbing liquids of two grades of spray systems injection above filler assembly 11 at filler assembly 11, absorb two grades of absorbing liquids of sulfur dioxide to fall into two grades and hold liquid bath 7, and recycled by secondary cycle pump 9 and secondary cycle pipeline 10, complete final sweetening process.By flue gas after the purification of filler assembly 11 by except mist assembly 13, after gas-liquid separation, discharge from dust-removal and desulfurizing reactor exhanst gas outlet 14.
Embodiment 1
Certain high-temperature flue-gas 180 DEG C, tolerance 180000Nm3/ h, SO2Concentration is 800mg/Nm3, dust content 500
mg/Nm3。
Reactor operating condition: operation temperature 170 DEG C, operates pressure normal pressure, and first order absorption liquid pH value is 6～7, and two grades of absorbing liquid pH value are 8～9.Rapids rushes liquid-gas ratio 6:1, and with NaOH solution as absorbent, gas-liquid counter current contacts；Filler assembly operation liquid-gas ratio 3:1.
After processed by the invention, flue-gas temperature 60 DEG C, desulfuration efficiency 98%, efficiency of dust collection 99%.
Claims (26)
1. a H type flue-gas dust-removing and desulfurization reactor, it is characterised in that described reactor includes pretreatment unit and advanced treatment unit, the two constitutes " H " type Double-Tower Structure；Wherein said pretreatment unit includes that smoke inlet, turbulent impulse scrubber, date core shaped structured packing assembly and one-level hold liquid bath from top to bottom, and described advanced treatment unit includes that two grades are held liquid bath, filler assembly, demister assembly and purifying smoke outlet from bottom to top；Described pretreatment unit is connected by the exhaust gases passes at middle part with advanced treatment unit；
Described date core shaped structured packing assembly includes at least date core shaped special pipe, and every layer of described some parallel connection, the date core shaped special pipe of horizontal positioned constitute multiple has collection section, aditus laryngis and the parallel channels of dispersion section；The both sides tube wall of date core shaped special pipe arranges some parallel, boss of protuberance.
2. according to the reactor described in claim 1, it is characterised in that adjacent two-layer date core shaped special pipe staggered, interval up and down shifts to install.
3., according to the reactor described in claim 1, it is characterised in that the cross section of described date core shaped special pipe is date core shaped, its top and bottom are acute triangle, and middle part is circular arc.
4. according to the reactor described in claim 1,2 or 3, it is characterised in that offer groove, described groove and boss interval on the both sides tube wall of described date core shaped special pipe bottom and arrange.
5., according to the reactor described in claim 1, it is characterised in that in described pretreatment unit, the wall top of reactor is provided with moisture film assembly.
6. according to the reactor described in claim 5, it is characterised in that the connecting portion in wall of reactor Yu smoke inlet reducing is provided with moisture film assembly.
7., according to the reactor described in claim 5 or 6, it is characterised in that arrange endless tube in wall of reactor surrounding, endless tube arranges the nozzle towards wall.
8. according to the reactor described in claim 6, it is characterized in that, described moisture film assembly is overflow-type moisture film assembly, the structure of overflow-type moisture film assembly is: the lower end of smoke inlet reducing connects one section of straight tube, the diameter of this direct tube section is more than the reactor diameter of pretreatment unit, forming, at wall of reactor and reducing connecting portion, the cannelure that a bottom lock, upper end are uncovered, this cannelure is held liquid bath with one-level and is connected by pipeline.
9. according to the reactor described in claim 8, it is characterised in that the uncovered employing tooth-shape structure of described cannelure.
10. according to the reactor described in claim 1, it is characterised in that the filler assembly in described advanced treatment unit selects structured packing assembly.
11. according to the reactor described in claim 10, it is characterised in that described filler assembly uses one layer of date core shaped special pipe structured packing.
12. according to the reactor described in claim 1, it is characterised in that described pretreatment unit also includes primary cycle pump and primary cycle pipeline；Described advanced treatment unit also includes secondary cycle pump, secondary cycle pipeline and two grades of spray systems.
13. according to the reactor described in claim 12, it is characterised in that two grades of described spray systems are positioned at above or below filler assembly.
14. according to the reactor described in claim 1, it is characterised in that described demister selects deflector type demister；Described deflector type demister includes that several are arranged side by side except mist assembly, each all includes riser and urceolus except mist assembly, and urceolus is arranged on the outside of riser, and with riser on the same axis；Riser is fixed on tower tray, and the top of riser arranges capping plate, and the circumference at riser has some seams, provided circumferentially about has the tangential flow guiding wing at the riser near each bar seam；Wherein said urceolus is made up of direct tube section and conical cylinder section.
15. according to the reactor described in claim 14, it is characterised in that the inner surface at described urceolus arranges projection.
16. according to the reactor described in claim 15, it is characterised in that described projection is hyoplastron, and the direction of rotation of hyoplastron is contrary with the direction of rotation of the tangential flow guiding wing.
17. according to the reactor described in claim 1, it is characterised in that places floating basket in the one-level of pretreatment unit holds liquid bath, places oxidation catalyst in floating basket.
18. 1 kinds of process for dusting and dsulfurizing fume, it is characterised in that the method use the arbitrary described H type flue-gas dust-removing and desulfurization reactor of claim 1 to 17.
19. according to the process for dusting and dsulfurizing fume described in claim 18, it is characterised in that described method includes herein below:
(1) high-temperature flue gas is after over-quenching is lowered the temperature, and enters pretreatment unit, is neutral or acid first order absorption liquid counter current contacting with the pH value of turbulent impulse scrubber ejection, carries out lowering the temperature, dedusting and pre-desulfurization；
(2) in step (1), flue gas after first order absorption continues with absorbing liquid and stream flows downward, and enters date core shaped structured packing assembly I, completes further absorbing the cooling of flue gas, dedusting and pre-desulfurization；
(3) the first order absorption liquid of sulfur dioxide absorption enters one-level and holds liquid bath, and is recycled by primary cycle pump and primary cycle pipeline；
(4) flue gas and after pretreatment unit absorbs enters advanced treatment unit, upwardly through filler assembly, and is fully contacted mass transfer with the pH value two grades of absorbing liquids in alkalescence at filler assembly, completes deep desulfurization process；
(5), by after the purification of filler assembly, flue gas is by demister, after gas-liquid separation, discharge from dust-removal and desulfurizing reactor exhanst gas outlet.
20. according to the process for dusting and dsulfurizing fume described in claim 19, it is characterised in that the SO in described flue gas2Concentration is 500～5000mg/Nm3, dust concentration is 200～800mg/Nm3。
21. according to the process for dusting and dsulfurizing fume described in claim 19, it is characterised in that the operating condition of described reactor is: operation temperature be 100～350 DEG C, operation pressure be normal pressure to 1MPa, treatment quantity is 500～200000m3/ h, absorbing liquid circulating load is 0.4m3/ h～7m3/h。
22. according to the process for dusting and dsulfurizing fume described in claim 19, it is characterised in that described absorbing liquid is NaOH solution, Na2CO3Solution, Mg (OH)2Solution or lime water Ca (OH)2。
23. according to the process for dusting and dsulfurizing fume described in claim 19, it is characterised in that the pH value of described first order absorption liquid is between 6～7, and described two grades of absorbing liquid pH value are between 8～10.
24. according to the process for dusting and dsulfurizing fume described in claim 20, it is characterised in that the SO in described flue gas2Concentration is 1000～4000mg/Nm3, dust concentration is 300～500mg/Nm3。
25. according to the process for dusting and dsulfurizing fume described in claim 21, it is characterised in that the operating condition of described reactor is: operation temperature is 150～200 DEG C, and treatment quantity is 700～190000 m3/ h, absorbing liquid circulating load is 0.5m3/ h～6m3/h。
26. according to the process for dusting and dsulfurizing fume described in claim 22, it is characterised in that described absorbing liquid is NaOH solution.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3841642A1 (en) * | 1988-12-10 | 1990-06-13 | Adam Muenzenberger Gmbh | Nozzle grating for gas scrubbers, absorbers and the like and column internal composed thereof |
| US6146597A (en) * | 1997-03-14 | 2000-11-14 | Petroleum Energy Center | Separation device |
| CN200995120Y (en) * | 2006-12-04 | 2007-12-26 | 无锡利保科技发展有限公司 | Smoke desulfurizing absorbing tower by integrated glass fiber reinforced plastic ammonia method |
| CN201299984Y (en) * | 2008-11-03 | 2009-09-02 | 山东科技大学 | High-speed three-dimensional mass-transfer tower plate with super-large air flow |
| CN101934192A (en) * | 2010-09-16 | 2011-01-05 | 江苏和亿昌环保工程科技有限公司 | Double-tower ammonia-method desulfurization process |
| CN202129016U (en) * | 2011-06-27 | 2012-02-01 | 朱岳虎 | Multifunctional desulfurization and denitrification integration device |
-
2013
- 2013-11-05 CN CN201310540366.3A patent/CN104607018B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3841642A1 (en) * | 1988-12-10 | 1990-06-13 | Adam Muenzenberger Gmbh | Nozzle grating for gas scrubbers, absorbers and the like and column internal composed thereof |
| US6146597A (en) * | 1997-03-14 | 2000-11-14 | Petroleum Energy Center | Separation device |
| CN200995120Y (en) * | 2006-12-04 | 2007-12-26 | 无锡利保科技发展有限公司 | Smoke desulfurizing absorbing tower by integrated glass fiber reinforced plastic ammonia method |
| CN201299984Y (en) * | 2008-11-03 | 2009-09-02 | 山东科技大学 | High-speed three-dimensional mass-transfer tower plate with super-large air flow |
| CN101934192A (en) * | 2010-09-16 | 2011-01-05 | 江苏和亿昌环保工程科技有限公司 | Double-tower ammonia-method desulfurization process |
| CN202129016U (en) * | 2011-06-27 | 2012-02-01 | 朱岳虎 | Multifunctional desulfurization and denitrification integration device |
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