CN101310827B - Activated charcoal gas cleaning method and device thereof - Google Patents
Activated charcoal gas cleaning method and device thereof Download PDFInfo
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- CN101310827B CN101310827B CN2008101008043A CN200810100804A CN101310827B CN 101310827 B CN101310827 B CN 101310827B CN 2008101008043 A CN2008101008043 A CN 2008101008043A CN 200810100804 A CN200810100804 A CN 200810100804A CN 101310827 B CN101310827 B CN 101310827B
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Abstract
The invention provides an active coke gas purifying method and a device thereof with high desulfurization and denitrification efficiency, energy conservation, little resistance of a bed layer, high utilization rate of the space in an absorption tower and low construction cost. The device comprises a main feed inlet and a gas main outlet which are arranged at the upper part of the absorption tower, a main discharge outlet and a gas main inlet which are arranged at the lower part of the absorption tower and an active coke bed layer which is positioned in the absorption tower, and the active coke bed layer is tilted and has an included angle Alpha with the vertical line. The method has the following steps: gas enters the active code bed layer from the gas main inlet, gas in the tilted bed layer is flowed to the top from the bottom; active coke simultaneously enters the active coke bed layer from the main feed inlet, the active coke in the tilted bed layer is flowed to the bottom from the top; the gas is exhausted from the gas main outlet after the fully tilted convection contact is formed between the gas and the active coke, and the active coke after the saturation by absorption can be discharged from the main discharge outlet.
Description
Technical field
The present invention relates to a kind of activated charcoal gas cleaning method and device.
Background technology
Active coke dry-method desulfuration, denitration technology often are applied to the industry coal-boiler gas cleaning, also are used in the absorption tower in fields such as chemical industry, metallurgy, glass, pharmacy gas cleaning and handle.
＜activated charcoal desulfur technology development 〉
The activated charcoal desulfur technology is to grow up the sixties in last century, based on dry desulfurization, the denitration technology of physical-chemical absorption principle, has that adsorption capacity is big, adsorption process and a fast advantage of catalytic conversion.The activated charcoal regeneration back of adsorbing sulfur dioxide is reusable, and the sulfur dioxide after the regeneration also can be made into byproducts such as sulfuric acid, sulfur dioxide liquid or elemental sulfur.In American-European, Japan and other countries, these technology process years of researches have had the commercial applications in a lot of fields, the activated coke absorption method is that German BF company was exploitation in 1967, then this technology (its scheme is the cross-flow absorption techniques) is introduced in the Mitsui Sumitomo, the WKV company that is come by German BF company's differentiation improves at the shortcoming of cross-flow technology, has invented at present the convection current absorption techniques of main flow in the world.
＜activated charcoal desulfur technology operation principle 〉
It is adsorbent that activated coke belongs to charcoal, has the characteristic of active carbon.Being that activated coke itself promptly is an adsorbent, is again catalyst, can also be used as catalyst carrier simultaneously.During flue gas process activated coke adsorption tower, the SO in the flue gas
2, NO
X, O
2, H
2The NH of O and feeding
3Be attracted in the activated coke hole.Under the activated coke catalytic action, SO
2And O
2And H
2O reacts, at last with H
2SO
4Form is attached in the activated coke hole; NO and O
2And NH
3Reaction generates N
2, NO
2With NH
3Reaction generates N
2Thereby, reach and remove SO in the coal-fired flue-gas
2And NO
XPurpose.
Two kinds of forms of＜present active coke desulphurizing technology 〉
Two kinds of forms that exist in present activated coke dry flue gas desulphurization, the denitration technology: a kind of is the cross-flow adsorption technology, and another kind is the convection current adsorption technology.The absorption principle of two kinds of technology is as follows:
Fig. 1 is a cross-flow adsorption technology structure principle chart, and the top, absorption tower is provided with fresh adsorbent import 24, and the bottom, absorption tower is provided with the saturated adsorbent outlet 25 of absorption, and the left side, absorption tower is provided with gas feed 26, and the right side, absorption tower is provided with gas vent 27.As shown in FIG., the adsorbent in the absorption tower can be divided into three zones, near in the zone 28 of gas feed 26 1 sides being the big adsorbent of absorption saturation degree; Near near gas vent 27 1 sides and be comparatively fresh adsorbent near the zone 29 the fresh adsorbent import 24; Near in the zone 30 of bottom, absorption tower being the saturated adsorbent of absorption.
The development of cross-flow adsorption technology is morning relatively, and from left to right by the absorption tower, activated coke is from top to bottom by the absorption tower in the side, absorption tower for gas, and the two cross-flow contacts.Advantage is: the air inlet area is big, gas air speed in tower is low, and bed resistance is little because in the tower air inlet need not be set, go out the headroom, activated coke storing and following material space, so space availability ratio is big in the absorption tower.Shortcoming: flue gas enters the activated coke bed from the side, adsorption reaction at first takes place and reaches capacity at first in the activated coke of close gas approach, flue gas is by moving from left to right, the absorption saturation capacity of activated coke reduces successively, total distribution situation is that the absorption saturation capacity of activated coke reduces from left to right successively, increase successively from top to bottom, less in activated coke adsorbance near smoke outlet one side, thereby make and contain some in the activated coke of discharge and do not adsorb activated coke completely, the activated coke that part is fresh is discharged from like this, and sent for regeneration, thereby the activated coke internal circulating load is strengthened, the increasing of internal circulating load also makes power consumption and breakage strengthen, the regenerative combustion gas amount strengthens, cause energy dissipation, because the activated coke adsorbance saturation capacity of bottom is bigger, desulfuration efficiency is lower in addition, top activated coke is because than comparatively fresh, desulfuration efficiency is higher, and total desulfurization of gas vent, denitration efficiency is the mean value of upper-lower position efficient, so its desulfurization, denitration efficiency is not as convection current adsorption efficiency height.
Fig. 2 is a convection current adsorption technology structure principle chart.The top, absorption tower is provided with fresh adsorbent import 24, and absorption tower bottom is provided with the adsorbent drain hole 39 of absorption after saturated, and the bottom, absorption tower is provided with gas feed 26, and top, absorption tower is provided with gas vent 27, is provided with adsorbent bed 33 in the absorption tower.Also comprise on the equipment as shown in the figure: active coke adsorbent warehouse 31, adsorbent uniform distribution device 32, adsorbent discharging opening and gas feed distributor 34, adsorbent blanking device 35, gas feed seal diaphragm 36, discharging controller 37, discharging warehouse 38.
The convection current adsorption technology is to allow flue gas upwards evenly pass the activated coke bed from the bottom, fresh activated coke flows downward from the top and contacts with gaseous exchange, thereby the activated coke absorption saturation capacity in the bed is reduced from down to up successively, adsorbing saturated activated coke at first is discharged from, adsorbance size for the activated coke on the same plane is identical, therefore the speed of activated coke decline also almost is the same, thereby the utilization rate of activated coke is improved greatly, and because the thickness of bed is uniform, the flue gas air inlet is also even, the resistance size of flue gas each point also is uniform, the time of contact of flue gas and activated coke is also basic identical, bed is long more high more time of contact, and desulfuration efficiency is also just high more, reaches as high as more than 99%.Blanking amount owing to each point in the tower in the convection techniques on the internal circulating load of activated coke is the same, and the activated coke particle of tower outlet nearly all is saturated, that is to say the SO of absorption as much
2, the activated coke that convection techniques is used is less relatively, and the activated coke of discharge is also just few, and promptly internal circulating load is little, and system is comparatively energy-conservation.Shortcoming is: because flue gas enters the absorption tower in the bottom, the air inlet area is less, and gas is the air speed height in tower, and bed resistance is big, simultaneously in tower, need to leave admission space, go out the headroom, activated coke storage bin, activated coke blanking bin, so space availability ratio is low in the convection current absorption tower.
The convection current adsorption technology is the adsorption technology of development after the cross-flow adsorption technology, and its advantage is adsorption efficiency height, active carbon utilization rate height; Its shortcoming is build process complexity, construction cost height.Because adopt the activated coke bed of convection current adsorption technology mostly to be flat shape, its floor space is bigger, need materials such as more steel during construction; Because adsorption plane is the plane, the activated coke recovery section need be provided with a plurality of valves and pipeline, complex structure, and the steel use amount is big, also breaks down easily.Generally under the situation of same flue gas treating capacity, the construction cost that adopts the convection current adsorption technology approximately is to adopt a times of construction cost of cross-flow adsorption technology.For example, build the adsorption plant that adsorption capacity is 2,200,000 standard cube exhaust gas volumns, adopting the construction cost of convection current adsorption technology approximately is 4.2 hundred million yuan, about 2.08 hundred million yuan of the construction cost of employing cross-flow adsorption technology.
[
Summary of the invention]
Technical problem to be solved by this invention is, provides a kind of desulfurization, denitration efficiency height, energy efficient and bed resistance is little, space availability ratio height in the absorption tower, activated charcoal gas cleaning method and device thereof that construction cost is low.
For solving the problems of the technologies described above, the present invention by the following technical solutions:
A kind of activated charcoal gas cleaning device, comprise the combined feed mouth, the gas general export that are positioned at top, absorption tower, total discharging opening of bottom, absorption tower, gas general import, and the activated charcoal bed that is positioned at the absorption tower, described activated charcoal bed is for tilting, and is an angle α between the vertical line of itself and horizontal plane.Described activated charcoal bed is separated into a plurality of tilting unit activated charcoal beds by the laminar flow dividing plate.The below of described unit activity coke bed is provided with the unitary gas import, is provided with the inlet gas passage between described unitary gas import and the gas general import; The top of described unit activity coke bed is provided with the unitary gas outlet, is provided with the exit gas passage between described unitary gas outlet and the gas general export; The top of described unit activity coke bed is provided with the unit feed mouth, and described unit feed mouth is connected with the combined feed mouth by unit feed mouth passage; The below of described unit activity coke bed is provided with the unit discharging opening, and described unit discharging opening is connected with total discharging opening by unit discharging opening passage.
Further, be provided with storage bin between described unit feed mouth passage and the combined feed mouth.
Further, the top of described unit activity coke bed is provided with the unit feed mouth, and described unit feed mouth is connected with main feeding-passage by unit feed mouth passage, and main feeding-passage is connected with the combined feed mouth.
Further, be provided with storage bin between described main charging aperture passage and the combined feed mouth.
Further, the below of described unit activity coke bed is provided with the unit discharging opening, described a plurality of unit discharging opening can be divided into some groups, each is organized the unit discharging opening and is connected with the one-level tapping channel by unit discharging opening passage, and described a plurality of one-level tapping channels are connected with total discharging opening by the secondary tapping channel.
Further, according to the quantity of unit activity coke bed, between secondary tapping channel and total discharging opening, three grades of tapping channels or the tapping channel more than three grades are set.
Further, the vertical range between two bottom surfaces up and down of described unit activity coke bed is H, floor projection distance between two sides at the unit air inlet of described unit activity coke bed and place, gas outlet, unit is L, and the ratio range of described vertical range H and floor projection distance L is: 0.4≤H:L≤2.
Further, the scope of described angle α is: 35 °≤α≤65 °.
Further, described unitary gas import is provided with the air inlet stop gauge; The air inlet stop gauge becomes miter angle with the horizontal plane vertical direction, and the air inlet stop gauge constitutes by being positioned at unitary gas import baffle plate all around.
Further, described unitary gas outlet is provided with the gas outlet stop gauge; The gas outlet stop gauge becomes miter angle with the horizontal plane vertical direction, and the gas outlet stop gauge constitutes by being positioned at unitary gas outlet baffle plate all around.
A kind of activated charcoal gas cleaning method, activated charcoal bed in the absorption tower is set to tilt, the top of described activated charcoal bed is provided with the gas general export, the combined feed mouth, the below of described unit activity coke bed is provided with gas general import, total discharging opening, and described method step is as follows:
Make gas enter the activated charcoal bed by the gas general import, in the tilting bed gas from below to above flow;
Make activated charcoal enter the activated charcoal bed simultaneously by the combined feed mouth, in the tilting bed activated charcoal from above to below flow;
After forming fully tiltedly convection current contact between gas and the activated charcoal, gas is discharged from the gas general export, adsorb activated charcoal after saturated from total discharging opening discharge.
Further, the activated charcoal bed is divided into the unit activity coke bed of a plurality of inclinations with the laminar flow dividing plate, the top of described unit activity coke bed is provided with the unitary gas outlet, the unit feed mouth, the below of described unit activity coke bed is provided with unitary gas import, unit discharging opening, and described method step is as follows:
Make gas enter each unit activity coke bed by the unit air inlet, in tilting unit bed gas from below to above flow;
Make activated charcoal enter each unit activity coke bed simultaneously by the unit feed mouth, in tilting unit bed activated charcoal from above to below flow;
After forming fully tiltedly convection current contact between gas and the activated charcoal, gas is discharged from the unitary gas outlet, and the activated charcoal that adsorbs after saturated is discharged from the unit discharging opening.
The present invention adopts laminar flow formula adsorption technology, compares with the cross-flow adsorption technology, and the adsorption efficiency of the technical scheme in the invention is significantly improved, and construction cost is more or less the same.With adopting the convection current adsorption technology to compare, the technical scheme among the present invention is under the situation of same adsorption efficiency, and construction cost just adopts about half of convection current adsorption technology, and saves steel, space availability ratio height, saving floor space.For example, build the adsorption plant that adsorption capacity is 2,200,000 standard cube exhaust gas volumns, adopting the construction cost of convection current adsorption technology approximately is 4.2 hundred million yuan, adopts the construction cost of technical solution of the present invention to be approximately 3.0 hundred million yuan, can save 1.2 hundred million yuan, reduce expenses 30% approximately.
The gas of purified treatment among the present invention can be the flue gas that industrial coal produces, also can other gas that need purify.
The invention has the beneficial effects as follows:
The advantage that has convection current adsorption technology and cross-flow adsorption technology simultaneously, desulfurization,
DenitrationEfficient height, bed resistance are little, activated coke absorbs that saturation degree is big, the little loss of internal circulating load is little, the regeneration energy consumption is low, space availability ratio height in the absorption tower, construction cost are low.
Description of drawings
Fig. 1 is a cross-flow adsorption technology structure principle chart;
Fig. 2 is a convection current adsorption technology structure principle chart;
Fig. 3 is the structural representation of the embodiment of the invention one;
Fig. 4 is that the embodiment of the invention one is along A-A direction left view;
Fig. 5 is that the embodiment of the invention one is along B-B direction right view;
Fig. 6 is the air inlet stop gauge structural representation of the embodiment of the invention one;
Fig. 7 is the gas outlet stop gauge structural representation of the embodiment of the invention one;
Fig. 8 is the embodiment of the invention one a unit activity coke bed structure proportion schematic diagram;
Fig. 9 is the feeding structure schematic diagram of the embodiment of the invention two;
Figure 10 is the discharging structure schematic diagram of the embodiment of the invention three;
In the accompanying drawing, the list of parts of each label representative is as follows:
1, unit feed mouth 2, unit activity coke bed 3, unitary gas import 4, unit discharging opening 5, unit discharge gate 6, gas general import 7, inlet gas passage 8, storage bin 9, gas general export 10, unitary gas outlet 11, shrouding 12, laminar flow dividing plate 13, gas outlet stop gauge 14, air inlet stop gauge 15, discharge gate pusher 16, combined feed mouth 17, unit feed mouth passage 18, unit discharging opening passage 19, exit gas passage 20, total discharging opening 21, main feeding-passage 22, one-level tapping channel 23, secondary feeding-passage 24, fresh adsorbent import 25, adsorb saturated adsorbent outlet 26, gas feed 27, gas vent 28, the big adsorbent 29 of absorption saturation degree, comparatively fresh adsorbent 30, adsorb saturated adsorbent 31, active coke adsorbent warehouse 32, adsorbent uniform distribution device 33, adsorbent bed 34, adsorbent discharging opening and gas inlet gas distributor 35, adsorbent blanking device 36, gas feed seal diaphragm car 37, discharging controller 38, discharging warehouse 39, adsorb the adsorbent drain hole after saturated
The specific embodiment
Below in conjunction with accompanying drawing principle of the present invention and feature are described, institute gives an actual example and only is used to explain the present invention, is not to be used to limit scope of the present invention.
As shown in Figure 3, the top on absorption tower is provided with combined feed mouth 16, and the below of combined feed mouth is provided with storage bin 8, and storage bin 8 internal memories are placed with fresh activated charcoal, top, absorption tower is provided with gas general export 9, and the bottom on absorption tower is provided with total discharging opening 20, gas general import 6.
Be provided with the activated charcoal bed in the absorption tower, the activated charcoal bed is for what tilt, and the activated charcoal bed is made of the unit activity coke bed 2 of a plurality of inclinations, is separated by laminar flow dividing plate 12 between each unit activity coke bed 2 and comes.Be parallel to each other between each unit activity coke bed 2, angle between each unit activity coke bed 2 and the vertical line is 45 °, also the angle α between unit activity coke bed 2 and the vertical line can be arranged to scope and be other angle of 35 °≤α≤65 °, to guarantee that activated charcoal can flow downward by gravity.
The oblique below of unit activity coke bed 2 is provided with equally distributed unitary gas import 3, is provided with inlet gas passage 7 between described unitary gas import 3 and the gas general import 6.Unitary gas import 3 is positioned at the absorption tower sidepiece, and flue gas enters inlet gas passage 7 by gas general import 6, enters unit activity charcoal bed 2 by unitary gas import 3 respectively then.The oblique upper of unit activity coke bed 2 is provided with equally distributed unitary gas outlet 10, is provided with exit gas passage 19 between described unitary gas outlet 10 and the gas general export 9.Purified gas is concentrated in the exit gas passage 19, is discharged by gas general export 9.
The oblique upper of unit activity coke bed 2 is provided with unit feed mouth 1, and unit feed mouth 1 is connected with the storage bin 8 that is positioned at combined feed mouth 16 belows by unit feed mouth passage 17, also can not establish storage bin, and promptly the unit feed mouth directly is connected with the combined feed mouth.The oblique below of unit activity coke bed 2 is provided with unit discharging opening 4, and unit discharging opening 4 is connected by unit discharging opening passage 18 with the total discharging opening 20 that is positioned at the bottom, absorption tower, and the end of each unit discharging opening passage 18 is unit discharge gate 5.
Shrouding 11 is in the both sides up and down on absorption tower, adopts the steel plate of tiling to make, and with wide identical, it plays sealing fume and supports the effect of tower body its size with the length on absorption tower.
As shown in Figure 4, a plurality of unit activity coke beds 2 distribute up and down side by side, on each unit activity coke bed 2 and column distribution a plurality of unitary gas imports 3, and a plurality of unit discharging opening passage 18 is interspersed between unitary gas import 3 and the unit discharging opening passage 18.
As shown in Figure 5, a plurality of unit activity coke beds 2 distribute up and down side by side, on each unit activity coke bed 2 and column distribution a plurality of unitary gas outlet 10, and a plurality of unit feed mouth passage 17 is interspersed between unitary gas outlet 10 and the unit feed mouth passage 17.
As shown in Figure 3, unitary gas import 3 is provided with air inlet stop gauge 14, and unitary gas outlet 10 is provided with gas outlet stop gauge 13.
As shown in Figure 6, air inlet stop gauge 14 becomes 45 degree with vertical direction, air inlet stop gauge 14 is made of the baffle plate that is positioned at around the unitary gas import 3, surrounds around it will unitary gas import 3, and air inlet stop gauge 14 can prevent that activated charcoal from leaking material at unitary gas import 3 places.
As shown in Figure 7, gas outlet stop gauge 13 becomes 45 degree with vertical direction, gas outlet stop gauge 13 is made of the baffle plate that is positioned at around the unitary gas outlet 10, and it will surround around the unitary gas outlet 10, and gas outlet stop gauge 13 can prevent that activated charcoal from exporting 10 places at unitary gas and leaking material.
As shown in Figure 8, the vertical range between two bottom surfaces up and down of unit activity coke bed is H, the floor projection distance that unit activity coke bed 2 exports at unitary gas import 3, unitary gas between two sides at 10 places is L, and the ratio range of described vertical range H and floor projection distance L is: 0.4≤H:L≤2.
As shown in Figure 3, the unit activity coke bed structure that above-mentioned layer-stepping tilts is symmetrical expression and distributes in the absorption tower.
When carrying out desulfurization, denitration, gas is from gas general import 6, through inlet gas passage 7, enters each unit activity coke bed 2 by unitary gas import 3 again, and gas flows to oblique upper below tiltedly in the tilting bed; Fresh activated charcoal enters storage bin 8 from combined feed mouth 16, enters each unit activity coke bed 2 by storage bin 8 through unit feed mouth passage 17, and activated charcoal flows below tiltedly from oblique upper; After forming fully oblique convection current contact between gas and the activated charcoal, purified gas is discharged from unitary gas outlet 10, and is concentrated in the exit gas passage 19, is discharged by gas general export 9; The activated charcoal that adsorbs after saturated is discharged from unit discharging opening 4, through unit discharging opening passage 18, discharges from total discharging opening 20.
Embodiment two
As shown in Figure 9, the difference of present embodiment and embodiment one is, feeding structure is provided with as follows: the top of unit activity coke bed 2 is provided with unit feed mouth 1, unit feed mouth 1 is connected with a main feeding-passage 21 by unit feed mouth passage 17, and main feeding-passage 21 is connected with the storage bin 8 that is positioned at combined feed mouth 16 belows.
Embodiment three
As shown in figure 10, the difference of present embodiment and embodiment one is, discharging structure is provided with as follows: the below of unit activity coke bed 2 is provided with unit discharging opening 1, a plurality of unit discharging opening 1 can be divided into some groups, each is organized unit discharging opening 1 and is connected with one-level tapping channel 22 by unit discharging opening passage 18, and above-mentioned a plurality of one-level tapping channels 22 are connected with total discharging opening 20 by secondary tapping channel 23.According to the quantity of unit activity coke bed, can also between secondary tapping channel 23 and total discharging opening 20, three grades of tapping channels or the tapping channel more than three grades be set.
In various embodiments of the present invention, each unit activity coke bed is provided with independently charging aperture and discharging opening to guarantee the absorption efficiency of each absorptive unit.In each unit activity coke bed, activated charcoal flows to oblique below from oblique upper, gas is from tiltedly the below is mobile obliquely upward, counter current contacting absorption, the adsorbent at each discharging opening place, unit all reaches the absorption saturation state, the gas absorption efficient of each unitary gas outlet is identical, adopts the side air inlet, and the air inlet area is big, bed resistance is less.The present invention has the advantage of adverse current adsorption technology and cross-flow adsorption technology simultaneously, desulfurization,
DenitrationEfficient height, bed resistance are little, activated coke absorbs that saturation degree is big, the little loss of internal circulating load is little, the regeneration energy consumption is low, space availability ratio height in the tower, construction cost are low.
The above only is embodiments of the present invention, be not so promptly limit claim of the present invention, the equivalent transformation that every utilization specification of the present invention and accompanying drawing content are done directly or indirectly is used in other relevant technical field, all in like manner is included in the claim of the present invention.
Claims (10)
1. activated charcoal gas cleaning device, comprise the combined feed mouth that is positioned at top, absorption tower, the gas general export, total discharging opening of bottom, absorption tower, the gas general import, and the activated charcoal bed that is positioned at the absorption tower, it is characterized in that, described activated charcoal bed is what tilt, be an angle α between the vertical line of itself and horizontal plane, described activated charcoal bed is separated into a plurality of tilting unit activated charcoal beds by the laminar flow dividing plate, the below of described unit activity coke bed is provided with the unitary gas import, is provided with the inlet gas passage between described unitary gas import and the gas general import; The top of described unit activity coke bed is provided with the unitary gas outlet, is provided with the exit gas passage between described unitary gas outlet and the gas general export; The top of described unit activity coke bed is provided with the unit feed mouth, and described unit feed mouth is connected with the combined feed mouth by unit feed mouth passage; The below of described unit activity coke bed is provided with the unit discharging opening, and described unit discharging opening is connected with total discharging opening by unit discharging opening passage.
2. activated charcoal gas cleaning device according to claim 1 is characterized in that, is provided with storage bin between described unit feed mouth passage and the combined feed mouth.
3. activated charcoal gas cleaning device according to claim 1, it is characterized in that, the top of described unit activity coke bed is provided with the unit feed mouth, and described unit feed mouth is connected with main feeding-passage by unit feed mouth passage, and main feeding-passage is connected with the combined feed mouth.
4. activated charcoal gas cleaning device according to claim 3 is characterized in that, is provided with storage bin between described main feeding-passage and the combined feed mouth.
5. activated charcoal gas cleaning device according to claim 1, it is characterized in that, the below of described unit activity coke bed is provided with the unit discharging opening, described a plurality of unit discharging opening can be divided into some groups, each is organized the unit discharging opening and is connected with the one-level tapping channel by unit discharging opening passage, and described a plurality of one-level tapping channels are connected with total discharging opening by the secondary tapping channel.
6. activated charcoal gas cleaning device according to claim 5 is characterized in that, according to the quantity of unit activity coke bed, between secondary tapping channel and total discharging opening three grades of tapping channels or the tapping channel more than three grades is set.
7. activated charcoal gas cleaning device according to claim 1, it is characterized in that, the vertical range between two bottom surfaces up and down of described unit activity coke bed is H, floor projection distance between two sides at the unit air inlet of described unit activity coke bed and place, gas outlet, unit is L, and the ratio range of described vertical range H and floor projection distance L is: 0.4≤H:L≤2.
8. activated charcoal gas cleaning device according to claim 1 is characterized in that, the scope of described angle α is: 35 °≤α≤65 °.
9. activated charcoal gas cleaning device according to claim 1 is characterized in that, described unitary gas import is provided with the air inlet stop gauge; The air inlet stop gauge becomes miter angle with the horizontal plane vertical direction, and the air inlet stop gauge constitutes by being positioned at unitary gas import baffle plate all around.
10. activated charcoal gas cleaning device according to claim 1 is characterized in that, described unitary gas outlet is provided with the gas outlet stop gauge; The gas outlet stop gauge becomes miter angle with the horizontal plane vertical direction, and the gas outlet stop gauge constitutes by being positioned at unitary gas outlet baffle plate all around.
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2008
- 2008-02-22 CN CN2008101008043A patent/CN101310827B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86104137A (en) * | 1986-12-15 | 1988-01-20 | 沈善明 | Moving bed activated carbon absorption-desorption device |
| CN1765471A (en) * | 2004-10-29 | 2006-05-03 | 张文辉 | Method for purifying flue gas by application of active coke |
| CN201168537Y (en) * | 2008-02-22 | 2008-12-24 | 张开元 | Active coke air purifying apparatus |
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