CN203400632U - Flue gas purification device - Google Patents
Flue gas purification device Download PDFInfo
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- CN203400632U CN203400632U CN201320390701.1U CN201320390701U CN203400632U CN 203400632 U CN203400632 U CN 203400632U CN 201320390701 U CN201320390701 U CN 201320390701U CN 203400632 U CN203400632 U CN 203400632U
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Abstract
The utility model relates to the field of flue gas purification treatment, and provides a flue gas purification device. The device comprises an adsorption tower and a regeneration tower, wherein the charging port of the adsorption tower is connected with the discharge port of the regeneration tower, and the discharge port of the adsorption tower is connected with the charging port of the regeneration tower; the adsorption tower comprises at least one adsorption module, at least one top storage tank and at least one bottom discharge tank; the adsorption module comprises a top storage bin, a denitration chamber, a desulfurization chamber and a bottom storage bin; the denitration chamber and the desulfurization chamber are communicated through an inlet blanking device; the inlet blanking device comprises an upper hopper, a lower hopper and a connecting pipe; the upper hopper and the lower hopper are of big end down hopper shapes; the upper opening of the upper hopper is communicated with the bottom of the denitration chamber; the lower hopper is sleeved on the upper hopper; a gap is reserved between the lower hopper and the upper hopper; the lower opening of the lower hopper is communicated with the upper end of the connecting pipe; the lower end of the connecting pipe is communicated with the top of the denitration chamber; and the bottom storage bin and the desulfurization chamber are communicated through the inlet blanking device. The device can keep a high-efficiency desulfurization capability, and can be used for removing oxynitride in flue gas.
Description
Technical field
The utility model relates to gas cleaning process field, particularly relate in a kind of sintering process of manufacturing for iron-smelter metal or fossil fuel (the coal)/coke in thermal power plant or the combustion process of its compound produce, in the flue gas of discharge, or the purifier of the flue gas discharging during the burning of industry/life waste material.
Background technology
In the flue gas that produces, discharges in sintering process in the manufacture of iron-smelter metal or fossil fuel (the coal)/coke in thermal power plant or the combustion process of its compound, or in the flue gas that industry/life waste material discharges while burning, contained SOx(oxysulfide), NOx(nitrogen oxide), (pollution sources such as heavy metal), bioxin/furans containing tribute, have caused serious pollution to environment to heavy metal.Chinese patent CN202289864U discloses a kind of dry desulfurization reaction tower, mainly comprise the grid being arranged in desulfurizing tower housing, desulfurizing tower is separated out to two-stage desulfurization agent layer, air inlet and air distributor are set between desulfurizing agent layer, it is provided with floss hole, gas outlet and charging door in top of desulfurizing agent layer at the middle and upper levels, and the bottom of lower floor's desulfurizing agent layer is provided with gas outlet and condensate drain mouth.Although above-mentioned desulfurization reaction tower can remove the oxysulfide in flue gas by loading active carbon, but because active carbon is immobilising, cause active carbon to use after a period of time, desulphurizing ability reduces, and this desulfurization reaction tower can not be removed the nitrogen oxide in flue gas.
Utility model content
The technical problems to be solved in the utility model is to provide a kind of smoke eliminator simple in structure, easy and simple to handle, can keep efficient desulphurizing ability, and can remove the nitrogen oxide in flue gas.
The utility model smoke eliminator, comprise adsorption tower and regenerator, the charging aperture of described adsorption tower is connected with the discharging opening of regenerator, the discharging opening of described adsorption tower is connected with the charging aperture of regenerator, described adsorption tower comprises at least one adsorption module, at least one top storage tank and at least one bottom discharge tank, each adsorption module includes top storage bin, denitration chamber, desulfurization chamber and bottom storage bin, denitration chamber is positioned at desulfurization chamber top, between denitration chamber and desulfurization chamber, be provided with into ammonia chamber, enter the bottom of ammonia chamber and the top of desulfurization chamber is connected, enter indoor at least one the first air inlet doffer that is provided with of ammonia, between denitration chamber and desulfurization chamber, by the first air inlet doffer, be communicated with, the first air inlet doffer comprises bucket, lower bucket and tube connector, upper bucket and lower bucket be big up and small down infundibulate all, the upper end open of upper bucket is communicated with the bottom of denitration chamber, on lower bucket is sleeved on and struggles against, between lower bucket and upper bucket, be provided with gap, the lower ending opening of lower bucket is communicated with the upper end of tube connector, the lower end of tube connector is communicated with the top of desulfurization chamber, bottom storage bin is positioned at desulfurization chamber below, between bottom storage bin and desulfurization chamber, be provided with bottom compartment, in bottom compartment, be provided with at least one second air inlet doffer, the second air inlet doffer is identical with the first air inlet doffer structure, between bottom storage bin and desulfurization chamber, by the second air inlet doffer, be communicated with, the upper end open of the upper bucket of the second air inlet doffer is communicated with the bottom of desulfurization chamber, the lower end of the tube connector of the second air inlet doffer is communicated with bottom storage bin, top storage bin is positioned at the top of denitration chamber, the top of denitration chamber is provided with at least one blanking funnel, the upper end of blanking funnel is communicated with top storage bin, the lower ending opening of blanking funnel is positioned at the top of denitration chamber, top storage tank is positioned at storage bin top, top, and be communicated with top storage bin, bottom discharge tank is positioned at storage bin below, bottom, and be communicated with bottom storage bin, top storage tank is connected with the charging aperture of adsorption tower, bottom discharge tank is connected with the discharging opening of adsorption tower, bottom in bottom compartment offers gas approach, entering on ammonia chamber, to offer ammonia injection apparatus, top in denitration chamber offers exhanst gas outlet, gas approach is communicated with the air inlet of adsorption tower, exhanst gas outlet is communicated with the gas outlet of adsorption tower.
The utility model smoke eliminator, wherein said adsorption tower comprises absorption module and support, absorption module comprises at least one adsorption module group, at least 1 top storage tank and at least 1 bottom discharge tank, adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part by a fixture, described movable part is positioned at the surrounding of fixture, fixture forms a fixed connection a little, movable part forms and is flexibly connected point, two parts up and down of described movable part can relatively move on horizontal plane, described in each, the top storage bin of adsorption module is all connected with four discharging openings of 1 tripper by 4 the second top fed pipes, each tripper charging aperture is all connected with top storage tank by 1 the first top fed pipe, the bottom storage bin of each adsorption module all logical charge tube is connected with bottom discharge tank.
The utility model smoke eliminator, wherein said absorption module comprises two adsorption module groups, before and after two adsorption module groups, arrange, between two adsorption module groups, air inlet pipe and escape pipe are set, one end of air inlet pipe is connected with the air inlet of adsorption tower, the other end of air inlet pipe is connected with the gas approach of each adsorption module, and one end of escape pipe is connected with the exhanst gas outlet of each adsorption module, and the other end of escape pipe is communicated with the gas outlet of adsorption tower.When absorption module is when more than two, absorption module is arranged side by side between any two, considers thermal expansion, has gap between two between adjacent absorption module.
The utility model smoke eliminator, also comprise regenerator and active device, the bottom discharge tank of described adsorption tower is connected with the charging aperture of active device, the discharging opening of described active device is connected with the charging aperture of regenerator, the discharging opening of described regenerator is connected with the top storage tank of adsorption tower, described active device comprises housing, transfer device and additive shower, and described additive shower is positioned at the top of transfer device, and the medicament of described additive shower spray is urea compounds.
The utility model smoke eliminator, also comprises fresh active carbon storage bin, and the discharging opening of described fresh active carbon storage bin is communicated with the charging aperture of regenerator.By fresh active carbon storage bin being connected to the charging aperture of regenerator, can remove moisture and fugitive constituent in fresh active carbon, increase its active function groups.
The utility model smoke eliminator, the active carbon that wherein said adsorption tower is used be by weight percent hundred for after brown coal 80% and bituminous coal 20% coordinates with tar, through charing, process final activated processing and making.
The utility model smoke eliminator, in wherein said adsorption tower, the flow velocity of smoke gas flow through desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
The utility model smoke eliminator difference from prior art is that the utility model is by arranging adsorption tower and regenerator, adsorption module is set in adsorption tower, desulfurization chamber and denitration chamber are set in an adsorption module, can effectively remove the sulfur and nitrogen oxides in flue gas, and by air inlet doffer, be communicated with between denitration chamber and desulfurization chamber, between bottom storage bin and desulfurization chamber, also by air inlet doffer, be communicated with, between top storage bin and denitration chamber, by blanking funnel, be communicated with, can guarantee that active carbon flows downward in purifying smoke, active carbon and flue gas form convection current, after being discharged from, active carbon after desulphurization denitration delivers to regenerator regeneration, active carbon after regeneration is admitted to adsorption tower charging aperture, for adsorption tower, reuse, formed the benign cycle of active carbon, guaranteed the desulphurization denitration ability of active carbon.
Below in conjunction with accompanying drawing, the utility model is described in further detail.
Accompanying drawing explanation
Fig. 1 is the structural representation of the adsorption module of the utility model smoke eliminator;
Fig. 2 is the structural representation of the adsorption tower of the utility model smoke eliminator;
Fig. 3 is the connection diagram of adsorption module and support in the utility model smoke eliminator;
Fig. 4 is the active carbon desulfurization power curve figure of the utility model smoke eliminator.
The specific embodiment
The utility model smoke eliminator comprises adsorption tower 4 and regenerator, and the charging aperture of adsorption tower 4 is connected with the discharging opening of regenerator, and the discharging opening of adsorption tower 4 is connected with the charging aperture of regenerator.
As shown in Figure 1, adsorption tower 4 comprises an adsorption module, a top storage tank 4s and a bottom discharge tank 4k, adsorption module includes top storage bin 4c, denitration chamber 4b, desulfurization chamber 4a and bottom storage bin 4l, denitration chamber 4b is positioned at desulfurization chamber 4a top, between denitration chamber 4b and desulfurization chamber 4a, be provided with into ammonia chamber 4g, the bottom of entering ammonia chamber 4g is connected with the top of desulfurization chamber 4a, enter and in the 4g of ammonia chamber, be provided with 4 the first air inlet doffer 4h, between denitration chamber 4b and desulfurization chamber 4a, by 4 the first air inlet doffer 4h, be communicated with, each first air inlet doffer 4h includes bucket 4h1, lower bucket 4h2 and tube connector 4h3, upper bucket 4h1 and lower bucket 4h2 be big up and small down infundibulate all, the upper end open of upper bucket 4h1 is communicated with the bottom of denitration chamber 4b, lower bucket 4h2 is sleeved on bucket 4h1, between lower bucket 4h2 and upper bucket 4h1, be provided with gap, so that flue gas enters the gap of active carbon or activated coke particle from the gap between bucket 4h1 and lower bucket 4h2.The lower ending opening of lower bucket 4h2 is communicated with the upper end of tube connector 4h3, the lower end of tube connector 4h3 is communicated with the top of desulfurization chamber 4a, thereby active carbon is entered in desulfurization chamber 4a through the first air inlet doffer 4h from denitration chamber 4b, and the flue gas on desulfurization chamber 4a top can, through entering after the 4g of ammonia chamber, enter in the 4b of denitration chamber by the gap between upper bucket 4h1 and lower bucket 4h2.
Bottom storage bin 4l is positioned at desulfurization chamber 4a below, between bottom storage bin 4l and desulfurization chamber 4a, be provided with the 4e of bottom compartment, in the 4e of bottom compartment, be provided with 4 the second air inlet doffer 4f, the second air inlet doffer 4f is identical with the first air inlet doffer 4h structure, between bottom storage bin 4l and desulfurization chamber 4a, by the second air inlet doffer 4f, be communicated with, the upper end open of the upper bucket of the second air inlet doffer 4f is communicated with the bottom of desulfurization chamber 4a, the lower end of the tube connector of the second air inlet doffer 4f is communicated with bottom storage bin 4l, so that flue gas gap between bucket and lower bucket from the second air inlet doffer 4f enters in desulfurization chamber 4a.
Flue gas is in flue-gas-cooling system is adjusted to adsorption tower after optimum treatmenting temperature scope, by air inlet, enter the gas approach 4d of adsorption tower 4 interior adsorption modules, at the 4e of bottom compartment, by the upper bucket of 4 the second air inlet doffer 4f that are evenly distributed and the gap between lower bucket, deliver to the desulfurization layer of desulfurization chamber 4a.The time stopping at desulfurization layer is according to some difference of the proterties of flue gas, best is that 0.2-0.3m/sec and inlet gas concentration are while being 150-220ppm through flow velocity, need the 4-7 time of staying of second, when inlet gas concentration is greater than 150-220ppm, the time of staying that need to be longer, if while surpassing this flow velocity 0.2-0.3m/sec, the dust of active carbon itself can disperse and be mixed in flue gas, the flue gas of meeting removing pollutant, in addition, flow velocity increase can cause the differential pressure of active carbon layer to increase.At desulfurization layer, by the adsorption function of active carbon or activated coke, remove the pollution sources such as oxysulfide, tribute, bioxin/furans.
Flue gas from desulfurization layer out after, the denitration floor that enters denitration chamber 4b through the first air inlet doffer 4h, is removed nitrogen oxide by catalysis by active carbon.Specifically, flue gas from desulfurization layer out, module enter ammonia chamber 4g in mix with ammonia, then enter the bottom of denitration layer.Ammonia is to discharge from ammonia storage tank with gaseous state, in atomizer, carry out heat exchange and heat up with steam, then the outer gas phase heating up with another kind of mode in blender is mixed mutually, and then the ammonia chamber 4g that enters in module mixes with flue gas by the ejection of ammonia injection apparatus is rear.The spray flux of ammonia is decided by the equivalent proportion of ammonia and nitrogen oxide, does not have the residue ammonia that can induce reaction with nitrogen oxide to regulate, in order to avoid surpass the standard value in environment permissible range.The time stopping at denitration layer is according to some difference of the proterties of flue gas, and best is 0.2-0.3m/sec and inlet gas concentration while being 150-220ppm through flow velocity, needs the 6-9 time of staying of second, when inlet gas concentration is greater than 150-220ppm, and the time of staying that need to be longer.In the 4b of denitration chamber, the nitrogen oxide in flue gas produces chemical reaction with ammonia selectively by the catalysis of active carbon, and resolves into water and nitrogen (N
2), then together pass through the exhanst gas outlet of adsorption module with the flue gas purifying, then by adsorption tower gas outlet, discharged, finally flow to chimney 7.
In order to improve the operating efficiency of adsorption tower 4, with respect to the adsorption tower 4 of above-described embodiment, do following improvement.In the present embodiment, adsorption tower 4 comprises absorption module and support, absorption module comprises two adsorption module groups, 1 top storage tank 4s and 4 bottom discharge tank 4k, adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, shown in Fig. 3, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part (being 5 movable parts in the present embodiment) by a fixture, movable part 31 is positioned at the surrounding of fixture 30, fixture 30 forms a fixed connection a little, movable part 31 forms and is flexibly connected point, two parts up and down of movable part can relatively move on horizontal plane, in the present embodiment, fixture is bolt, movable part is lower plate, pillar and ball bearing, lower plate is fixedly mounted on the top of the adsorption module that is positioned at below, pillar upper end is fixedly mounted on the bottom of the adsorption module that is positioned at top, ball bearing is equipped with roll mode in pillar lower end, ball bearing is pressed on the upper surface of lower plate.Shown in figure 1, the top storage bin 4c of each adsorption module is all connected with four discharging openings of 1 tripper 4j by 4 the second top fed pipe 4m, each tripper 4j is all connected with top storage tank 4s by 1 the first top fed pipe 4t, described in each the bottom storage bin 4l of adsorption module all logical charge tube be connected with bottom discharge tank 4k.
As shown in Figure 2, when processing a large amount of flue gas, normally 6m is wide, 6m long for the size of single-bit module, and maximum is also that 7.2m is wide, and 7.2m is long, adsorption tower comprises two of left and right absorption module, if absorption module is two, consider thermal expansion when above, should leave suitable interval, therefore, in the present embodiment, between two absorption modules, there is certain interval.Each absorption module includes two adsorption module groups, and namely an adsorption tower includes 16 adsorption modules.Before and after two adsorption module groups, arrange, air inlet pipe 4q and escape pipe 4r are set between two adsorption module groups, one end of air inlet pipe 4q is connected with the air inlet of adsorption tower, the other end of air inlet pipe 4q is connected with the gas approach 4d of each adsorption module, one end of escape pipe 4r is connected with the exhanst gas outlet 4i of each adsorption module, and the other end of escape pipe 4r is communicated with the gas outlet of adsorption tower 4.By two storage tanks are only set on adsorption tower, have greatly reduced like this each module and had indivedual regulative modes of storage tank (" module, a storage tank ") separately in the hidden danger of machinery, operating aspect.And the bifurcated of active carbon material feeding pipeline and conveying equipment and distributor become simpler, distance becomes the shortest.Three-temperature sensor is all installed in each adsorption module.
Adsorption module is due to structure and the loading of filling the active carbon in it is subject to vertically, the impact of horizontal loading, during running, the temperature of flue gas makes its inside usually maintain the temperature conditions of 120-150 ° of C, therefore need to think about the impact of loading and thermal expansion, then using optimal module number as its base unit.In the present embodiment with 8 adsorption modules, the absorption module of take is base unit, between the absorption module of two of left and right, leave expansion joint space, by expansion joint, the air inlet pipe of two absorption modules is connected with escape pipe, and the bottom of adsorption module is connected with support with 5 movable parts by a fixture, above-mentioned thermal expansion is dropped to minimum on the impact of adsorption tower mechanical performance, when emergency occurs, (when " focus " occurs) guarantees the absolute construction that other adsorption towers are immune.
The bottom discharge tank 4k of adsorption tower 4 is connected with the charging aperture of active device, the discharging opening of active device is connected with the charging aperture of regenerator, the discharging opening of regenerator is connected with the top storage tank 4s of adsorption tower 4, active device comprises housing, transfer device and additive shower, additive shower is fixedly mounted in housing, and additive shower is positioned at the top of transfer device, active carbon is from the charging aperture of active device enters, by transfer device (as belt conveyor), be transferred to the discharging opening of active device, in this process, additive shower is to spraying agent on active carbon, the medicament of additive shower spray is urea compounds.The discharging opening of fresh active carbon storage bin is communicated with the charging aperture of regenerator.
The active carbon of discharging from adsorption module is processed through regeneration to regenerator, and the pollution sources such as oxysulfide, tribute and bioxin/furans that are adsorbed on active carbon become concentrated gas; Oxysulfide is made business sulfuric acid in sulfuric acid manufacturing equipment, and other pollution sources are processed in sewage treatment equipment.Bioxin in regenerating active carbon process, high temperature in regenerator (400-450 ° of C) and no oxygen (O
2) condition under decompose completely, eliminate.
Active carbon through regenerating in regenerator, its most pollution sources have been resolved and have decomposed, conventionally make to remain in wherein less than the micropollution source of 1wt%, discharging opening place at regenerator arranges sieve, thereby the active carbon size after assurance regeneration is just transported in adsorption tower 4 and re-uses more than maintaining 2.8mm.The dust arrester that the active carbon of regeneration and new active carbon together arrange by adsorption tower top is housed in the storage tank 4s of top after removing fine dust.The pipeline that active carbon is connected along top storage bin 4c against gravity from top storage tank moves down, action by switch baffle plate on pipeline and pipeline remains airtight successively, and then the second top fed pipe 4m via module top enters in the storage bin 4c of top.Be contained in after the active carbon material feeding in the storage bin of top, at denitration chamber 4b, by catalysis, carry out denitration (denitrogenation), at desulfurization chamber 4a, by adsorption function, carry out desulfurization, in these denitrations and sweetening process, active carbon suitably stays for some time, and then in order to regenerate, from the desulfurization chamber 4a of module, discharges.Active carbon temporarily leaves in bottom storage bin 4l and bottom discharge tank 4k after discharging from desulfurization chamber 4a according to the time of programming on time, then with carrying equipment, discharges.
Active carbon after active device spray and be together delivered to regenerator from the fresh active carbon of fresh active carbon storage bin supply, raises from top through heating zone temperature in order to regenerate, and starts to resolve when temperature surpasses 300 ° of C.The concentrated sulfur dioxide forming heating zone temperature is raised to 400-450 ° of C and resolves, decomposes from active carbon, together through degas zone, is delivered to sulfuric acid manufacturing equipment with other resolved pollution sources.Active carbon completes after parsing in degas zone, move down into bottom coohng district, the outer gas of being introduced by pressure fan carries out cooling, in addition gas is obtained thermal source and is heated up by heat exchange in the process of cooling active carbon, about 200-250 ° C, be heated to again 500-600 ° of C in heat riser after, move on to heating zone, the temperature of active carbon is raise, finally from regenerator, deliver to atmosphere.Active carbon is from regenerator is discharged, and through sifting out, the active carbon that is only greater than 2.8mm enters in adsorption tower again, the active carbon micro mist leaching or other collection of granule less than 2.8mm, re-uses from sieve.According to the amounts of activated carbon from system filtering, from fresh active carbon storage bin, supply the fresh active carbon of same amount.
Active carbon in adsorption module is as the medium of removing pollution sources in flue gas, need to form benign cycle, in other words, in adsorption tower, by round and smooth discharging and charging, the pollution sources in adsorption tower are extracted out and regenerated rapidly, then the active carbon of regeneration is fed intake again, and the active carbon of discharging in adsorption tower is when stop, for fear of phenomenons such as dewfall and corrosion, occur, the discharge rate of active carbon and internal circulating load, with iron-smelter sinter fume sulphur oxide concentration, 220ppm is as the criterion, and comparing with the active carbon total amount of whole module should be within the scope of 0.15-0.2wt%; Active carbon is carried the maximum machine ability of equipment, and comparing with active carbon total amount should be within the scope of 0.3 – 0.4wt%; Sulfoxide concentration is higher, and the machine capability of internal circulating load and conveying equipment should be improved accordingly.Active carbon is under the state of the pollution sources such as absorption oxysulfide, when stopping for a long time in adsorption tower 4, regenerator and other storage tanks, for fear of occurring in phenomenons such as the following dewfall/corrosion of acid dew point, heater, insulation are taked to and/or with measures such as nitrogen fillings in the outside of container, reduce and the contacting of oxygen.Active carbon has high abrasiveness, for fear of the mechanical wear generation of carrying equipment activated carbon granule to be pulverized completely or weakened, should select friction can be dropped to minimum equipment.Conventionally to use the low abrasiveness such as bucket conveyor, flexible rubber conveyer belt to carry equipment.When carrying active carbon, likely there is hidden danger in forward and backward technique, therefore the surge tank of suitable capacity need to be installed to pooling feature can be provided; Active carbon and be attracted to pollution sources wherein in adsorption tower 4, regenerator and other storage tanks during long-term stop, takes heater, insulation and/or with measures such as nitrogen fillings, in order to avoid in phenomenon generations such as the following dewfall/corrosion of acid dew point to container.
The active carbon that the utility model is used is to be, after brown coal 80% and bituminous coal 20% coordinate with tar (pitch), through charing, to process by percentage by weight, finally through activation processing, makes.Certainly, the utility model also can be used other active carbons or activated coke.
Existing active carbon, active carbon of the present utility model and the active carbon of the present utility model after chemokinesis have been carried out to the test to oxysulfide adsorption capacity, and measured the oxysulfide being adsorbed in active carbon.Result of the test is presented in accompanying drawing 4.The active carbon of the present utility model activating after chemical addition agent sprays is stronger than other two kinds of active carbons to the adsorption capacity of oxysulfide.After it should be noted that active carbon of the present utility model activates, in absorption and parsing circulation repeatedly, its oxysulfide adsorption capacity remains well, never goes down.This result of the test shows, the active carbon using in flue gas purification system its machinery and chemical characteristic in circulation technology are repeatedly faded.Active carbon of the present utility model after chemokinesis will improve following functions: improve SWC(desulfurization load factor); By keeping chemical group, reduce active carbon wearing and tearing; Avoid the inner clogging of adsorption tower to occur; In the denitrification process of adsorption tower, reduce ammonia consumption.
Above-described embodiment is described preferred embodiment of the present utility model; not scope of the present utility model is limited; do not departing under the prerequisite of the utility model design spirit; various distortion and improvement that those of ordinary skills make the technical solution of the utility model, all should fall in the definite protection domain of the utility model claims.
Claims (7)
1. a smoke eliminator, comprises adsorption tower (4) and regenerator, and the charging aperture of described adsorption tower (4) is connected with the discharging opening of regenerator, and the discharging opening of described adsorption tower (4) is connected with the charging aperture of regenerator, it is characterized in that:
Described adsorption tower (4) comprises at least one adsorption module, at least one top storage tank (4s) and at least one bottom discharge tank (4k), described each adsorption module includes top storage bin (4c), denitration chamber (4b), desulfurization chamber (4a) and bottom storage bin (4l), described denitration chamber (4b) is positioned at desulfurization chamber (4a) top, between described denitration chamber (4b) and desulfurization chamber (4a), be provided with into ammonia chamber (4g), the bottom of entering ammonia chamber (4g) is connected with the top of desulfurization chamber (4a), describedly enter in ammonia chamber (4g) to be provided with at least one first air inlet doffer (4h), between described denitration chamber (4b) and desulfurization chamber (4a), by the first air inlet doffer (4h), be communicated with, described the first air inlet doffer (4h) comprises bucket (4h1), lower bucket (4h2) and tube connector (4h3), described upper bucket (4h1) and lower bucket (4h2) be big up and small down infundibulate all, the upper end open of described upper bucket (4h1) is communicated with the bottom of denitration chamber (4b), described lower bucket (4h2) is sleeved on bucket (4h1), between lower bucket (4h2) and upper bucket (4h1), be provided with gap, the lower ending opening of lower bucket (4h2) is communicated with the upper end of tube connector (4h3), the lower end of tube connector (4h3) is communicated with the top of desulfurization chamber (4a), described bottom storage bin (4l) is positioned at desulfurization chamber (4a) below, between described bottom storage bin (4l) and desulfurization chamber (4a), be provided with bottom compartment (4e), in described bottom compartment (4e), be provided with at least one second air inlet doffer (4f), described the second air inlet doffer (4f) is identical with the first air inlet doffer (4h) structure, between described bottom storage bin (4l) and desulfurization chamber (4a), by the second air inlet doffer (4f), be communicated with, the upper end open of the upper bucket of described the second air inlet doffer (4f) is communicated with the bottom of desulfurization chamber (4a), the lower end of the tube connector of the second air inlet doffer (4f) is communicated with bottom storage bin (4l), described top storage bin (4c) is positioned at the top of denitration chamber (4b), the top of described denitration chamber (4b) is provided with at least one blanking funnel (4n), the upper end of described blanking funnel (4n) is communicated with top storage bin (4c), the lower ending opening of blanking funnel (4n) is positioned at the top of denitration chamber (4b), described top storage tank (4s) is positioned at top storage bin (4c) top, and be communicated with top storage bin (4c), described bottom discharge tank (4k) is positioned at bottom storage bin (4l) below, and be communicated with bottom storage bin (4l), described top storage tank (4s) is connected with the charging aperture of adsorption tower, described bottom discharge tank (4k) is connected with the discharging opening of adsorption tower, in the bottom of described bottom compartment (4e), offer gas approach (4d), described, enter on ammonia chamber (4g) to offer ammonia injection apparatus, at the top of denitration chamber (4b), offer exhanst gas outlet (4i), described gas approach (4d) is communicated with the air inlet of adsorption tower (4), described exhanst gas outlet (4i) is communicated with the gas outlet of adsorption tower (4).
2. smoke eliminator according to claim 1, it is characterized in that: described adsorption tower (4) comprises absorption module and support, described absorption module comprises at least one adsorption module group, at least 1 top storage tank (4s) and at least 1 bottom discharge tank (4k), described adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part by a fixture, described movable part is positioned at the surrounding of fixture, fixture forms a fixed connection a little, movable part forms and is flexibly connected point, two parts up and down of described movable part can relatively move on horizontal plane, described in each, the top storage bin (4c) of adsorption module is all connected with four discharging openings of 1 tripper (4j) by 4 the second top fed pipes (4m), each tripper (4j) charging aperture is all connected with top storage tank (4s) by 1 the first top fed pipe (4t), described in each the bottom storage bin (4l) of adsorption module all logical charge tube be connected with bottom discharge tank (4k).
3. smoke eliminator according to claim 2, it is characterized in that: described absorption module comprises two adsorption module groups, before and after two adsorption module groups, arrange, air inlet pipe (4q) and escape pipe (4r) are set between two adsorption module groups, one end of described air inlet pipe (4q) is connected with the air inlet of adsorption tower, the other end of air inlet pipe (4q) is connected with the gas approach (4d) of each adsorption module, one end of described escape pipe (4r) is connected with the exhanst gas outlet (4i) of each adsorption module, the other end of described escape pipe (4r) is communicated with the gas outlet of adsorption tower (4).
4. smoke eliminator according to claim 3, is characterized in that: when described absorption module is when more than two, absorption module between any two left and right is arranged side by side, and has gap between two between adjacent absorption module.
5. smoke eliminator according to claim 4, it is characterized in that: also comprise regenerator and active device, the bottom discharge tank (4k) of described adsorption tower (4) is connected with the charging aperture of active device, the discharging opening of described active device is connected with the charging aperture of regenerator, the discharging opening of described regenerator is connected with the top storage tank (4s) of adsorption tower (4), described active device comprises housing, transfer device and additive shower, described additive shower is positioned at the top of transfer device, and the medicament of described additive shower spray is urea compounds.
6. smoke eliminator according to claim 5, is characterized in that: also comprise fresh active carbon storage bin, the discharging opening of described fresh active carbon storage bin is communicated with the charging aperture of regenerator.
7. smoke eliminator according to claim 1, is characterized in that: the flow velocity of the interior smoke gas flow of described adsorption tower (4) through desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320390701.1U CN203400632U (en) | 2013-07-02 | 2013-07-02 | Flue gas purification device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320390701.1U CN203400632U (en) | 2013-07-02 | 2013-07-02 | Flue gas purification device |
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| CN203400632U true CN203400632U (en) | 2014-01-22 |
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| CN201320390701.1U Withdrawn - After Issue CN203400632U (en) | 2013-07-02 | 2013-07-02 | Flue gas purification device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103405982A (en) * | 2013-07-02 | 2013-11-27 | 香港诺曼泰壹环保科技有限公司 | Smoke purification device |
| CN106861422A (en) * | 2015-12-13 | 2017-06-20 | 天津赫维科技有限公司 | A kind of processing method of industrial nitrous oxides exhaust gas |
| CN114917714A (en) * | 2022-04-22 | 2022-08-19 | 山东保蓝环保工程有限公司 | Normal-pressure carbon dioxide adsorption tank |
-
2013
- 2013-07-02 CN CN201320390701.1U patent/CN203400632U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103405982A (en) * | 2013-07-02 | 2013-11-27 | 香港诺曼泰壹环保科技有限公司 | Smoke purification device |
| CN106861422A (en) * | 2015-12-13 | 2017-06-20 | 天津赫维科技有限公司 | A kind of processing method of industrial nitrous oxides exhaust gas |
| CN114917714A (en) * | 2022-04-22 | 2022-08-19 | 山东保蓝环保工程有限公司 | Normal-pressure carbon dioxide adsorption tank |
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