CN103405982B - Smoke purification device - Google Patents
Smoke purification device Download PDFInfo
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- CN103405982B CN103405982B CN201310274797.XA CN201310274797A CN103405982B CN 103405982 B CN103405982 B CN 103405982B CN 201310274797 A CN201310274797 A CN 201310274797A CN 103405982 B CN103405982 B CN 103405982B
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- 239000000779 smoke Substances 0.000 title claims abstract description 30
- 238000000746 purification Methods 0.000 title abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 61
- 238000007599 discharging Methods 0.000 claims abstract description 29
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 69
- 229910052799 carbon Inorganic materials 0.000 claims description 61
- 230000003009 desulfurizing Effects 0.000 claims description 59
- 239000007789 gas Substances 0.000 claims description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 28
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 27
- 239000003546 flue gas Substances 0.000 claims description 27
- 238000010521 absorption reaction Methods 0.000 claims description 23
- 238000000034 method Methods 0.000 claims description 15
- 239000000654 additive Substances 0.000 claims description 11
- 230000000996 additive Effects 0.000 claims description 11
- 239000003610 charcoal Substances 0.000 claims description 11
- 230000000694 effects Effects 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 6
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 239000002802 bituminous coal Substances 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 3
- 239000003077 lignite Substances 0.000 claims description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea group Chemical group NC(=O)N XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 25
- 230000008929 regeneration Effects 0.000 abstract description 10
- 238000011069 regeneration method Methods 0.000 abstract description 10
- 229910052813 nitrogen oxide Inorganic materials 0.000 abstract description 9
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000011068 load Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 150000002240 furans Chemical class 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 230000001590 oxidative Effects 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 230000010002 chemokinesis Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- 241000628997 Flos Species 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- 238000001994 activation Methods 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 125000003636 chemical group Chemical group 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000011176 pooling Methods 0.000 description 1
- 230000001172 regenerating Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 150000003462 sulfoxides Chemical class 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
The invention relates to a smoke purification device which belongs to the field of smoke purification treatment. The smoke purification device provided by the invention comprises an adsorption tower and a regeneration tower, wherein a feeding port of the adsorption tower is connected with a discharging port of the regeneration tower; a discharging port of the adsorption tower is connected with a feeding 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, and the adsorption module comprises a top storage bin, a denitration chamber, a desulfuration chamber and a bottom storage bin; the denitration chamber is communicated with the desulfuration chamber through an air inlet blanking device which comprises an upper hopper, a lower hopper and a connecting pipe, each of the upper hopper and the lower hopper is shaped like a funnel which has larger upper part and smaller lower part, and an opening in the upper end 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, an opening in the lower end 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 desulfuration chamber, and the bottom storage bin is communicated with the desulfuration chamber through the air inlet blanking device. The device provided by the invention has the advantages that the high-efficiency desulfuration capability can be kept, and nitrogen oxides in smoke is removed.
Description
Technical field
The present invention relates to smoke, particularly relate in a kind of flue gas for producing in the 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, discharging, or the purifier of the flue gas discharged during industry/life waste incineration.
Background technology
Produce in sintering process during iron-smelter metal manufactures or fossil fuel (the coal)/coke in thermal power plant or the combustion process of its compound, in the flue gas of discharge, or in the flue gas discharged during industry/life waste incineration, contained SOx(oxysulfide), NOx(nitrogen oxide), heavy metal (containing the pollution sources such as heavy metal), bioxin/furans of tribute, causes serious pollution to environment.Chinese patent CN202289864U discloses a kind of dry desulfurization reaction tower, mainly comprise the grid be arranged in desulfurizing tower housing, desulfurizing tower is separated out two-stage desulfurization oxidant layer, air inlet and air distributor are set between desulfurization oxidant layer, the top of its desulfurizing agent layer is at the middle and upper levels provided with floss hole, gas outlet and charging door, and the bottom of lower floor's desulfurization oxidant layer is provided with gas outlet and condensate drain mouth.Although above-mentioned desulfurization reaction tower can remove the oxysulfide in flue gas by filling active carbon, but because active carbon is immobilising, after causing active carbon to use a period of time, desulphurizing ability reduces, and this desulfurization reaction tower can not remove the nitrogen oxide in flue gas.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of structure smoke eliminator simple, easy and simple to handle, can keep efficient desulphurizing ability, and can remove the nitrogen oxide in flue gas.
Smoke eliminator of the present invention, 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 above desulfurization chamber, be provided with into ammonia room between denitration chamber and desulfurization chamber, the top of the bottom and desulfurization chamber of entering ammonia room is connected, enter ammonia indoor and be provided with at least one first air inlet doffer, be communicated with by the first air inlet doffer between denitration chamber with desulfurization chamber, first air inlet doffer comprises bucket, lower bucket and tube connector, upper bucket and all big up and small down infundibulate of lower bucket, the upper end open of upper bucket is communicated with the bottom of denitration chamber, on lower bucket is sleeved on and struggles against, gap is provided with between lower bucket and upper bucket, the lower lower ending opening of 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 below desulfurization chamber, bottom compartment is provided with between bottom storage bin and desulfurization chamber, at least one second air inlet doffer is provided with in bottom compartment, second air inlet doffer is identical with the first air inlet doffer structure, be communicated with by the second air inlet doffer between bottom storage bin with desulfurization chamber, the upper end open of 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 above top storage bin, and be communicated with top storage bin, bottom discharge tank is positioned at below bottom storage bin, 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, gas approach is offered in the bottom of bottom compartment, entering on ammonia room to offer ammonia injection apparatus, exhanst gas outlet is offered at the top of denitration chamber, gas approach is communicated with the air inlet of adsorption tower, exhanst gas outlet is communicated with the gas outlet of adsorption tower.
Smoke eliminator of the present invention, 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, also be fixedly connected with between upper and lower two-layer adsorption module, 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 is formed and is flexibly connected point, two parts up and down of described movable part can relative movement in the horizontal plane, the top storage bin of each described adsorption module is all connected with four discharging openings of 1 tripper by 4 second its top feed pipes, each tripper charging aperture is all connected with top storage tank by 1 first its top feed pipe, the all logical charge tube of bottom storage bin of each adsorption module is connected with bottom discharge tank.
Smoke eliminator of the present invention, wherein said absorption module comprises two adsorption module groups, arrange before and after two adsorption module groups, 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 two or more, absorption module between any two left and right is arranged side by side, and considers thermal expansion, there is gap between absorption module adjacent between two.
Smoke eliminator of the present invention, 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.
Smoke eliminator of the present invention, also comprises fresh activity charcoal storage bin, and the discharging opening of described fresh activity charcoal storage bin is communicated with the charging aperture of regenerator.By fresh activity charcoal storage bin being connected to the charging aperture of regenerator, the moisture in fresh activity charcoal and fugitive constituent can being removed, increase its active function groups.
Smoke eliminator of the present invention, the active carbon that wherein said adsorption tower uses is by weight percent hundred for after brown coal 80% and bituminous coal 20% coordinates with tar, through charing process, final activated process and making.
Smoke eliminator of the present invention, in wherein said adsorption tower, flue gas flows through the flow velocity of desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
Smoke eliminator difference from prior art of the present invention is that the present invention passes through to arrange adsorption tower and regenerator, in adsorption tower, adsorption module is set, in an adsorption module, desulfurization chamber and denitration chamber are set, effectively can remove the sulfur and nitrogen oxides in flue gas, and be communicated with by air inlet doffer between denitration chamber with desulfurization chamber, also be communicated with by air inlet doffer between bottom storage bin with desulfurization chamber, be communicated with by blanking funnel between top storage bin with denitration chamber, can ensure that active carbon flows downward while purifying smoke, active carbon and flue gas form convection current, regenerator regeneration is delivered to after active carbon after desulphurization denitration is discharged, active carbon after regeneration is admitted to adsorption tower charging aperture, reuse for adsorption tower, define the benign cycle of active carbon, ensure that the desulphurization denitration ability of active carbon.
Below in conjunction with accompanying drawing, the invention will be further described.
Accompanying drawing explanation
Fig. 1 is the structural representation of the adsorption module of smoke eliminator of the present invention;
Fig. 2 is the structural representation of the adsorption tower of smoke eliminator of the present invention;
Fig. 3 is the connection diagram of adsorption module and support in smoke eliminator of the present invention;
Fig. 4 is the active carbon desulfurization power curve figure of smoke eliminator of the present invention.
Detailed description of the invention
Smoke eliminator of the present invention 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 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 above desulfurization chamber 4a, be provided with into ammonia room 4g between denitration chamber 4b and desulfurization chamber 4a, the bottom entering ammonia room 4g is connected with the top of desulfurization chamber 4a, enter in the 4g of ammonia room to be provided with 4 the first air inlet doffer 4h, be communicated with by 4 the first air inlet doffer 4h between denitration chamber 4b with desulfurization chamber 4a, each first air inlet doffer 4h includes bucket 4h1, lower bucket 4h2 and tube connector 4h3, the infundibulate that upper bucket 4h1 and lower bucket 4h2 is all big up and small down, the upper bucket upper end open of 4h1 is communicated with the bottom of denitration chamber 4b, lower bucket 4h2 is sleeved on bucket 4h1, gap is provided with between lower bucket 4h2 and upper bucket 4h1, 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, thus make active carbon enter in desulfurization chamber 4a from denitration chamber 4b through the first air inlet doffer 4h, and the flue gas on desulfurization chamber 4a top after entering ammonia room 4g, can be entered in denitration chamber 4b by the gap between upper bucket 4h1 and lower bucket 4h2.
Bottom storage bin 4l is positioned at below desulfurization chamber 4a, bottom compartment 4e is provided with between bottom storage bin 4l and desulfurization chamber 4a, 4 the second air inlet doffer 4f are provided with in bottom compartment 4e, second air inlet doffer 4f is identical with the first air inlet doffer 4h structure, be communicated with by the second air inlet doffer 4f between bottom storage bin 4l with desulfurization chamber 4a, 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, enter in desulfurization chamber 4a from the gap between the upper bucket and lower bucket of the second air inlet doffer 4f to make flue gas.
Top storage bin 4c is positioned at the top of denitration chamber 4b, the top of denitration chamber 4b is provided with 4 blanking funnel 4n, the upper end of 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, enters in denitration chamber 4b through blanking funnel 4n to enable the active carbon in top storage bin 4c.Top storage tank 4s is positioned at above top storage bin 4c, and is communicated with top storage bin 4c.Bottom discharge tank 4k is positioned at below bottom storage bin 4l, and is communicated with bottom storage bin 4l, and top storage tank 4s is connected with the charging aperture of adsorption tower, and bottom discharge tank 4k is connected with the discharging opening of adsorption tower.Gas approach 4d is offered in the bottom of bottom compartment 4e, entering on the 4g of ammonia room to offer ammonia injection apparatus, offer exhanst gas outlet 4i at the top of denitration chamber 4b, gas approach 4d is communicated with the air inlet of adsorption tower 4, and exhanst gas outlet 4i is communicated with the gas outlet of adsorption tower 4.
Flue gas to be adjusted in adsorption tower after optimum treatmenting temperature scope through flue-gas-cooling system, the gas approach 4d of adsorption module in adsorption tower 4 is entered by air inlet, at bottom compartment 4e by the gap between the upper bucket of 4 the second air inlet doffer 4f be evenly distributed and lower bucket, deliver to the desulfurization layer of desulfurization chamber 4a.In the time that desulfurization layer stops according to some difference of the proterties of flue gas, best be 0.2-0.3 m/sec and inlet gas concentration is 150-220 ppm through flow velocity, need the time of staying of 4-7 second, when inlet gas concentration is greater than 150-220 ppm, need the time of staying more grown, if when exceeding this flow velocity 0.2-0.3 m/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, remove the pollution sources such as oxysulfide, tribute, bioxin/furans by the adsorption function of active carbon or activated coke.
Flue gas from desulfurization layer out after, through the denitration layer that the first air inlet doffer 4h enters denitration chamber 4b, nitrogen oxide is removed by catalysis by active carbon.Specifically, flue gas from desulfurization layer out, mixes with ammonia in entering in the 4g of ammonia room of module, then enters the bottom of denitration layer.Ammonia is discharged from ammonia storage tank with gaseous state, in atomizer, carry out heat exchange with steam and heat up, then the outer gas phase heated up with another kind of mode in a mixer mixes mutually, then mixes with flue gas by the ejection of ammonia injection apparatus is rear at the ammonia room 4g that enters of module.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 need to regulate, in order to avoid exceed the standard value in environment permissible range.In the time that denitration layer stops according to some difference of the proterties of flue gas, best be 0.2-0.3 m/sec and inlet gas concentration is 150-220 ppm through flow velocity, need the time of staying of 6-9 second, when inlet gas concentration is greater than 150-220 ppm, need the time of staying more grown.In denitration chamber 4b, 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 with purification flue gas together through the exhanst gas outlet of adsorption module, then discharged by adsorption tower gas outlet, finally flow to chimney 7.
In order to improve the operating efficiency of adsorption tower 4, do following improvement relative to the adsorption tower 4 of above-described embodiment.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, also be fixedly connected with between upper and lower two-layer adsorption module, shown in composition graphs 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 is formed and is flexibly connected point, two parts up and down of movable part can relative movement in the 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 being positioned at below, pillar upper end is fixedly mounted on the bottom of the adsorption module being positioned at top, lower rod end is equipped with ball bearing with roll mode, 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 second its top feed pipe 4m, each tripper 4j is all connected with top storage tank 4s by 1 first its top feed pipe 4t, and all logical charge tube of bottom storage bin 4l of each described adsorption module is 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, left and right absorption module, if when absorption module is two or more, considers thermal expansion, suitable interval should be left, therefore, between two absorption modules, there is certain interval in the present embodiment.Each absorption module includes two adsorption module groups, and namely an adsorption tower includes 16 adsorption modules.Arrange before and after two adsorption module groups, air inlet pipe 4q and escape pipe 4r is 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 only arranging two storage tanks on adsorption tower, greatly reduce the hidden danger of indivedual regulative modes in machinery, operating aspect that each module has respective storage tank (" module, a storage tank ") like this.And the bifurcated of active carbon material feeding pipeline and conveying equipment and distributor become simpler, and distance becomes the shortest.In each adsorption module, all three-temperature sensor is installed.
Adsorption module is subject to impact that is vertical, horizontal loading due to structure and the loading of filling the active carbon in it, during running, the temperature of flue gas makes its inner temperature conditions usually maintaining 120-150 ° of C, therefore the impact thinking about loading and thermal expansion is needed, then using optimal module number as its base unit.With 8 adsorption modules in the present embodiment, namely module is adsorbed for base unit with one, expansion joint space is left between two, left and right absorption module, be connected with escape pipe by the air inlet pipe of expansion joint by two absorption modules, and the bottom of adsorption module is connected with support with 5 movable parts by a fixture, the impact of above-mentioned thermal expansion on adsorption tower mechanical performance is dropped to minimum, and when emergency occurs, (when " focus " occurs) ensures 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, after active carbon enters from the charging aperture of active device, the discharging opening of active device is transferred to by transfer device (as belt conveyor), 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 activity charcoal storage bin is communicated with the charging aperture of regenerator.
The active carbon of discharging from adsorption module processes through regeneration to regenerator, and the pollution sources such as absorption oxysulfide on the activated carbon, tribute and bioxin/furans become concentrated gas; Oxysulfide makes business sulfuric acid in sulfuric acid manufacturing equipment, and other pollution sources process in sewage treatment equipment.Bioxin in regenerating active carbon process, high temperature (400-450 ° of C) and no oxygen (O in regenerator
2) condition under decompose completely, eliminate.
Through the active carbon of regeneration in regenerator, the resolved Sum decomposition of its most pollution sources, usually the micropollution source less than 1 wt% is made to remain in wherein, in the discharge outlet of regenerator, sieve is set, thus ensure that the active carbon size after regeneration maintains more than 2.8mm, be just transported in adsorption tower 4 and re-use.The dust arrester that the active carbon of regeneration and new active carbon are together arranged by adsorption tower top is housed in top storage tank 4s after removing fine dust.The pipeline that active carbon is connected against gravity from top storage tank along top storage bin 4c moves down, remain airtight successively by the action of switch baffle plate on pipeline and pipeline, the second its top feed pipe 4m then via module top enters in top storage bin 4c.After being contained in the active carbon material feeding in top storage bin, denitration (denitrogenation) is carried out by catalysis at denitration chamber 4b, desulfurization is carried out by adsorption function at desulfurization chamber 4a, in these denitrations and sweetening process, active carbon suitably stays for some time, and then discharges from the desulfurization chamber 4a of module to regenerate.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 discharges with carrying equipment.
Active carbon after active device spray and be together delivered to regenerator from the fresh activity charcoal of fresh activity charcoal storage bin supply, in order to regenerate from top through heating zone and temperature raises, when temperature is resolved more than starting during 300 ° of C.Be raised to 400-450 ° of C in heating zone temperature and resolve, decompose the concentrated sulfur dioxide of rear formation from active carbon, with other resolved pollution sources together through degas zone, being delivered to sulfuric acid manufacturing equipment.Active carbon is after degas zone completes parsing, move down into bottom coohng district, the outer gas introduced by pressure fan cools, in addition gas obtains thermal source by heat exchange and heats up in the process of cooling active carbon, about 200-250 ° C, move on to heating zone be heated to 500-600 ° of C again in heat riser after, the temperature of active carbon is raised, finally delivers to air from regenerator.After active carbon is discharged from regenerator, through sifting out, the active carbon being only greater than 2.8mm enters in adsorption tower again, the active carbon micro mist leached from sieve or re-use after collecting in addition less than the granule of 2.8mm.According to the amounts of activated carbon from system filtering, from fresh activity charcoal storage bin, supply the fresh activity charcoal of identical amount.
Active carbon in adsorption module is as the medium removing pollution sources in flue gas, benign cycle need be formed, in other words, by round and smooth discharging and charging the pollution sources in adsorption tower extracted out rapidly in adsorption tower and regenerate, then the active carbon of regeneration is fed intake again, and when the active carbon of discharging in adsorption tower stops, in order to avoid the phenomenons such as condensation and corrosion occur, the discharge rate of active carbon and internal circulating load, be as the criterion with iron-smelter sinter fume sulphur oxide concentration 220ppm, should within the scope of 0.15-0.2 wt% compared with the active carbon total amount of whole module; The maximum machine ability of active carbon conveying equipment, should within the scope of 0.3-0.4 wt% compared with active carbon total amount; 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, in adsorption tower 4, regenerator and other storage tanks when long-term stop, in order to avoid below acid dew point, the phenomenon such as condensation/corrosion occurs, heater, insulation and/or with measures such as nitrogen fillings are taked to the outside of container, reduces the contact with oxygen.Active carbon has high abrasiveness, to be pulverized completely by activated carbon granule or the mechanical wear that weakens occurs in order to avoid conveying equipment, should select friction can be dropped to minimum equipment.Usually the low abrasiveness conveying such as bucket conveyor, flexible rubber conveyer belt equipment will be used.When conveying active carbon, likely there is hidden danger in forward and backward technique, therefore needs the surge tank installing suitable capacity can provide pooling feature; When active carbon and the pollution sources be attracted to wherein stop for a long time in adsorption tower 4, regenerator and other storage tanks, heater, insulation and/or with measures such as nitrogen fillings are taked to container, in order to avoid the phenomenon generation such as condensation/corrosion below acid dew point.
The active carbon that the present invention uses is, after brown coal 80% and bituminous coal 20% coordinate with tar (pitch), through charing process, eventually pass through activation process and make by percentage by weight.Certainly, the present invention also can use other active carbons or activated coke.
Existing active carbon, active carbon of the present invention and the active carbon of the present invention after chemokinesis are carried out the test to oxysulfide adsorption capacity, and measures the oxysulfide be adsorbed in active carbon.Result of the test display in figure 4.The active carbon of the present invention activated 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 invention 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 used in flue gas purification system its machinery and chemical characteristic in circulation technology are repeatedly faded.Active carbon of the present invention after chemokinesis will improve following functions: improve SWC(desulfurization load factor); By keeping chemical group, reduce active carbon wearing and tearing; The inner clogging of adsorption tower is avoided to occur; Ammonia consumption is reduced in the denitrification process of adsorption tower.
Above-described embodiment is only be described the preferred embodiment of the present invention; not scope of the present invention is limited; under not departing from the present invention and designing the prerequisite of spirit; the various distortion that those of ordinary skill in the art make technical scheme of the present invention and improvement, all should fall in protection domain that claims of the present invention determines.
Claims (8)
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, be provided with between described denitration chamber (4b) and desulfurization chamber (4a) into ammonia room (4g), the bottom entering ammonia room (4g) is connected with the top of desulfurization chamber (4a), describedly enter to be provided with at least one first air inlet doffer (4h) in ammonia room (4g), be communicated with by the first air inlet doffer (4h) between described denitration chamber (4b) with desulfurization chamber (4a), described first air inlet doffer (4h) comprises bucket (4h1), lower bucket (4h2) and tube connector (4h3), described upper bucket (4h1) and all big up and small down infundibulate of lower bucket (4h2), 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), gap is provided with between lower bucket (4h2) and upper bucket (4h1), 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, bottom compartment (4e) is provided with between described bottom storage bin (4l) and desulfurization chamber (4a), at least one second air inlet doffer (4f) is provided with in described bottom compartment (4e), described second air inlet doffer (4f) is identical with the first air inlet doffer (4h) structure, be communicated with by the second air inlet doffer (4f) between described bottom storage bin (4l) with desulfurization chamber (4a), the upper end open of the upper bucket of described 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, gas approach (4d) is offered in the bottom of described bottom compartment (4e), enter ammonia room (4g) offers ammonia injection apparatus described, exhanst gas outlet (4i) is offered at the top of denitration chamber (4b), 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, also be fixedly connected with between upper and lower two-layer adsorption module, 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 is formed and is flexibly connected point, two parts up and down of described movable part can relative movement in the horizontal plane, the top storage bin (4c) of each described adsorption module is all connected with four discharging openings of 1 tripper (4j) by 4 second its top feed pipes (4m), each tripper (4j) charging aperture is all connected with top storage tank (4s) by 1 first its top feed pipe (4t), the all logical charge tube of bottom storage bin (4l) of each described adsorption module is 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, arrange before and after two adsorption module groups, 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 two or more, and absorption module between any two left and right is arranged side by side, and there is gap between absorption module adjacent between two.
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 activity charcoal storage bin, and the discharging opening of described fresh activity charcoal storage bin is communicated with the charging aperture of regenerator.
7. smoke eliminator according to claim 1, is characterized in that: the active carbon that described adsorption tower (4) uses is after brown coal 80% and bituminous coal 20% coordinate with tar by percentage by weight, through charing process, and final activated process and making.
8. smoke eliminator according to claim 1, is characterized in that: the flow velocity that described adsorption tower (4) interior flue gas flows through desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
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| CN201310274797.XA CN103405982B (en) | 2013-07-02 | 2013-07-02 | Smoke purification device |
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| CN201310274797.XA CN103405982B (en) | 2013-07-02 | 2013-07-02 | Smoke purification device |
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| CN103405982B true CN103405982B (en) | 2015-04-22 |
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| CN104624030B (en) * | 2015-01-28 | 2018-04-10 | 邹炎 | Gas purification filler bed apparatus |
| CN107185404A (en) * | 2017-07-13 | 2017-09-22 | 中国科学院过程工程研究所 | A kind of gas cleaning absorption tower and its flue gas purifying method and application |
| CN110559851A (en) * | 2019-09-30 | 2019-12-13 | 中冶东方工程技术有限公司 | Ultra-low temperature modularization flue gas denitration system |
| CN112403192B (en) * | 2020-10-29 | 2022-07-26 | 攀枝花市蓝鼎环保科技有限公司 | Sintering flue gas treatment device capable of simultaneously performing desulfurization and denitrification |
| CN114832594B (en) * | 2021-02-01 | 2023-03-24 | 中国石油化工股份有限公司 | Efficient treatment device and treatment method for hydrogen sulfide tail gas |
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| US6863875B1 (en) * | 1998-04-13 | 2005-03-08 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating system and process |
| CN102824809B (en) * | 2012-09-21 | 2015-05-13 | 中冶长天国际工程有限责任公司 | Adsorption tower |
| CN103007735B (en) * | 2012-10-30 | 2015-08-26 | 上海克硫环保科技股份有限公司 | A kind of high-efficiency activated burnt system for desulfuration and denitration and method |
| CN202860399U (en) * | 2012-10-30 | 2013-04-10 | 上海克硫环保科技股份有限公司 | Efficient desulfuration and denitration system for active cokes |
| CN203400632U (en) * | 2013-07-02 | 2014-01-22 | 香港诺曼泰壹环保科技有限公司 | Flue gas purification device |
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