CN202762307U - Axial and radial cross-flow moving bed type adsorption reactor for smoke desulphurization and denitration utilizing activated coke - Google Patents
Axial and radial cross-flow moving bed type adsorption reactor for smoke desulphurization and denitration utilizing activated coke Download PDFInfo
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- CN202762307U CN202762307U CN2012204872462U CN201220487246U CN202762307U CN 202762307 U CN202762307 U CN 202762307U CN 2012204872462 U CN2012204872462 U CN 2012204872462U CN 201220487246 U CN201220487246 U CN 201220487246U CN 202762307 U CN202762307 U CN 202762307U
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- activated coke
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- moving bed
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- 239000000571 coke Substances 0.000 title claims abstract description 95
- 239000000779 smoke Substances 0.000 title claims abstract description 15
- 239000002245 particle Substances 0.000 claims abstract description 19
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000006477 desulfuration reaction Methods 0.000 claims description 49
- 230000003009 desulfurizing Effects 0.000 claims description 49
- 210000000498 stratum granulosum Anatomy 0.000 claims description 39
- 230000000274 adsorptive Effects 0.000 claims description 33
- 230000037361 pathway Effects 0.000 claims description 12
- 239000007921 spray Substances 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 8
- 239000011236 particulate material Substances 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000008187 granular material Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 30
- 239000003344 environmental pollutant Substances 0.000 abstract description 7
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052753 mercury Inorganic materials 0.000 abstract description 7
- 238000000746 purification Methods 0.000 abstract description 6
- 231100000719 pollutant Toxicity 0.000 abstract description 5
- 239000007787 solid Substances 0.000 abstract description 4
- 238000002156 mixing Methods 0.000 abstract description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract 1
- 206010022000 Influenza Diseases 0.000 abstract 1
- 229910002089 NOx Inorganic materials 0.000 abstract 1
- 238000002347 injection Methods 0.000 abstract 1
- 239000007924 injection Substances 0.000 abstract 1
- 239000002912 waste gas Substances 0.000 abstract 1
- 239000003546 flue gas Substances 0.000 description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 35
- 238000000034 method Methods 0.000 description 7
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 6
- 235000011130 ammonium sulphate Nutrition 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000009856 non-ferrous metallurgy Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- -1 sulphur ammonium salt Chemical compound 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000005039 chemical industry Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 210000004907 Glands Anatomy 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000001174 ascending Effects 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000006704 dehydrohalogenation reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 230000001473 noxious Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000002588 toxic Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000001131 transforming Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
An axial and radial cross-flow moving bed type adsorption reactor for smoke desulphurization and denitration utilizing activated coke mainly realizes combined removal and integral purification of pollutants such as SO2, NOx, mercury, dioxin and the like in smoke and belongs to the technical field of comprehensive treatment of waste gas in flues. The adsorption reactor is a combined double-section double-n-shaped axial and radial cross-flow moving bed; the lower section of the reactor is a desulphurization region which is divided into a rough desulphurization region and a fine desulphurization region, and is provided with an inner circular activated coke particle layer and an outer circular activated coke particle layer; the upper section of the reactor is a denitration region provided with one activated coke particle layer; an ammonia injection pipe is disposed between the upper section and the lower section; a smoke inlet is of a double-port circular air channel structure, smoke in the lower section flows centripetally to be subjected to desulphurization and smoke in the upper section flows centrifugally to be subjected to denitration. Desulphurization and denitration are realized by the same adsorption reactor, and the adsorption reactor has the advantages of efficient utilization of activated coke, uniform mixing of smoke, sufficient contact of gas and solid, running stability and reliability, running cost economization and the like.
Description
Technical field
The utility model belongs to stack gases process for comprehensively treating field, and the flue gas desulfurization, denitration, demercuration, Tuo bioxin, the dedusting that relate to the fields such as Coal-fired Thermal Power, coal-burning boiler, iron making and sintering machine, nonferrous metallurgy and chemical building material (contain PM
2.5) and cigarette (giving up) the gas integrated purification technology of dehydrohalogenation, particularly the activated coke desulfurization denitration diameter of axle is to cross-flow moving bed adsorptive reactor.
Background technology
Industrialized fast development has promoted social scientific and technological progress high speed development, yet human when enjoying scientific and technological achievement, the various problem of environmental pollutions that also bearing fossil fuel and cause.Be discharged into SO a large amount of in the atmosphere every year
2And NO
xCause serious acid rain harm.Therefore, in " 12 " with in afterwards longer time, China control SO
2And NO
xThe task of discharging and energy-saving and emission-reduction is very heavy, and larger desulfurization and the denitration market demand are arranged.Increasingly strict along with to environmental requirement, be discharged in the atmosphere mercury He the noxious materials such as bioxin also begin to receive publicity and control, to Air Pollution Control from before simple flue gas desulfurization change gradually flue gas desulfurization, denitration, demercuration into Yu uniting of the multi-pollutants such as bioxin removes.
The poor sulphur of China, annual cost huge fund is from a large amount of sulphur of external import, and need a large amount of chemical fertilizer every year on China's agricultural, and industrial trade also needs a large amount of sulfuric acid.Simultaneously, the primary energy of China is take coal as main, Coal-fired Thermal Power, coal-burning boiler, and the industry such as chemical industry, iron and steel, nonferrous metallurgy, building materials is to the more SO of airborne release
2And NO
x, cause the wasting of resources and Air seriously polluted.Therefore, exploitation can unite remove, flue gases purification that resource reclaims is significant to environmental protection cause.NORTHWEST CHINA and North China are the areas that coal reserves distributes and enriches.The Coal-fired Thermal Power electric power stations near coal-mines that China newly increases mainly concentrates on the water shortage in north china area, needs the highly flue gas desulfurization technique of water saving of development.Resources for construction economizing type, environmentally friendly society greatly develop green economy, are the problems that China's present stage development must be faced.
Radially moving bed and the diameter of axle to moving bed be a kind of in petrochemical industry and chemical industry widely used reactor, in the adsorption and desorption process, also obtain application, had low pressure drop, gas distribution is even, particle moving is even, be easy to maximize, the advantage such as stable.But the system air speed in the radially moving bed processing of petrochemical industry is high, is not suitable for the active coke desulphurizing denitrification process of low-speed process.Patent ZL200810104398.8 discloses a kind of radially moving bed for gas cleaning, it is reported, radially moving bed with activated coke do not expect the envelope, desulfurization section activated coke layer only arranges a particle moving speed, do not distinguish thick desulfurization and smart desulfurization, the activated coke utilization rate is low; Add the spray ammonia entrance of ammonia on the top of tower when denitration, the position is higher, mixes fully not with flue gas, requires further improvement.The reactor of the combined desulfurization and denitration of some unit exploitations of Japan and Germany, be used widely, but have still that gas-solid contact is insufficient, a focus easily emerges in the bed, the multiple-unit multiple module paralleling is so that the shortcoming such as device is complicated, particularly gas material envelope section activated coke utilization rate is lower, the activated coke hierarchy is unreasonable, the cloth air chamber is bigger than normal, and the upper-lower section composite behaviour is on the low side etc., causes gas cleaning effect and equipment effectiveness that improved space is arranged.
Summary of the invention
The purpose of this utility model is to overcome the shortcomings such as gas-solid contact is insufficient in the background technology, activated coke is low in sealing gland section utilization rate, the activated coke layering is efficient and rational not, the upper-lower section composite behaviour is on the low side, provide a kind of activated coke desulfurization denitration diameter of axle to cross-flow moving bed adsorptive reactor, realize the SO in the flue gas
2, NO
x, mercury He uniting of the pollutants such as bioxin remove and integrated purifying.
To achieve these goals, the technical solution adopted in the utility model is:
A kind of activated coke desulfurization denitration diameter of axle is to cross-flow moving bed adsorptive reactor, comprise and placing in the described reactor wall, and by epimere denitration district and the hypomere desulfurization zone of the upper and lower separation of dividing plate, it is characterized in that: described hypomere desulfurization zone ecto-entad is equipped with hypomere annular airflow runner, outer Johnson Net, outer grid, front activated coke stratum granulosum, middle Johnson Net, middle grid, rear activated coke stratum granulosum, interior Johnson Net, center tube wall, central tube mass flow pathway successively; The built-in activated coke stratum granulosum in described epimere denitration district communicates with front activated coke stratum granulosum in the hypomere desulfurization zone by intersegmental front particle blanking pipe, communicates with described rear activated coke stratum granulosum by intersegmental rear particle blanking pipe;
The front activated coke stratum granulosum that described hypomere desulfurization zone is built-in and rear activated coke stratum granulosum top, the below of described dividing plate, described reactor wall side from up to down are equipped with gas approach and a plurality of humidifying cooling nozzle successively; The top of activated coke stratum granulosum below, described epimere denitration district, described dividing plate, described reactor wall from up to down is equipped with exhanst gas outlet successively and ammonia sprays into pipe.
Described gas approach quantity has two, is the twoport annular airflow road structure that liquidates, and is equipped with a plurality of smoke gas flows on the annular airflow road and portals, and top, annular airflow road is dividing plate, and epimere denitration district and hypomere desulfurization zone are separated, and prevents from that air-flow from altering to walk to epimere denitration district.
It is 2～4 that described ammonia sprays into pipe, is distributed on the periphery of the same aspect on the described reactor wall, and described ammonia sprays into pipe and is connected with intersegmental gas flow tube by check valve and communicates, and prevents the refluence of flue gas in the central tube runner.
Described humidifying cooling nozzle quantity is 4～8, the uniform periphery that is arranged in the same aspect of described reactor wall.
The upper end of described middle Johnson Net and center tube wall is equipped with respectively axially annular granule material block plate different in size, the length of the interior ring particulate material block plate that the upper end of described center tube wall is equipped with, length greater than the outer shroud particulate material block plate that is equipped with on the described middle Johnson Net, the built-in activated coke stratum granulosum in described epimere denitration district is the outside at two ends up and down, be equipped with annular granule material block plate, the air-flow that forms is when the hypomere centripetal flow and the activated coke particulate material envelope of air-flow when the epimere centrifugal flow, cause air-flow the diameter of axle to occur to two-dimensional flow in activated coke material envelope section, increased the loadings of activated coke in activated coke utilization rate and the unit volume equipment.
Epimere annular airflow mass flow pathway and hypomere annular airflow runner adopt sector drum or outer screen member.
In the described adsorptive reactor stratum granulosum particle commutator is set.
The top of the bottom of epimere denitration district activated coke stratum granulosum and hypomere desulfurization zone activated coke stratum granulosum is separately installed with central tube and strengthens bracing frame; The up and down two ends of central tube are equipped with the central tube supporting seat and are guaranteed the stable of structure.
Between intersegmental gas flow tube and activated coke stratum granulosum, because remaining SO
2With NH
3Reaction, can generate a small amount of ammonium sulfate, the a small amount of sulphur ammonium salt that generates can increase mobile viscous force in activated coke, therefore cleaning inner member or manhole are set in device, regularly clear up, and by the connection of screening pipe vibratory sieve is set at the adsorptive reactor hypomere, when separating broken activated coke and coke powder, also sieve out a part of ammonium sulfate, by above-described method ammonium sulfate is removed, reduce the viscous force in the activated coke motion.
The utility model diameter of axle compared with prior art has the following advantages to cross-flow moving bed adsorptive reactor:
In a reactor, realize SO
2, NO
x, mercury He uniting of the pollutants such as bioxin remove;
Activated coke particulate material envelope and air-flow the activated coke particulate material envelope when epimere centrifugal flow of air-flow when the hypomere centripetal flow, cause air-flow the diameter of axle to occur to two-dimensional flow in activated coke material envelope section, increased the loadings of activated coke in activated coke utilization rate and the unit volume equipment;
The hypomere desulfurization zone is divided into thick desulfurization zone and smart desulfurization zone is separated design, by the regulation particle moving speed of valve, guarantees that particle moving is even, has realized the efficient utilization of activated coke and the high-efficiency desulfurization of device;
The design of ammonia entry position has increased the incorporation time of flue gas ammonia in the inner uphill process of central tube, makes gas-solid contact more abundant, and prevents that by the setting of valve flue gas from flowing backwards;
Gas approach adopts the form that liquidates, and flows out by the perforate in described annular airflow road during through annular airflow road gas distribution, realizes the uniform target of ejection;
Continuously stable, save equipment investment and operating cost.
Description of drawings
Below the utility model is described in further detail by the specific embodiment and description of drawings.
Fig. 1 is the utility model adsorptive reactor structural representation;
Fig. 2 is the A-A cross-sectional view (epimere denitration district, the gas centrifugation direction flows) among Fig. 1;
Fig. 3 is B-B cross-sectional view among Fig. 1 (ammonia admission line, valve control);
Fig. 4 is C-C cross-sectional view among Fig. 1 (gas approach and annular airflow road structure);
Fig. 5 is D-D cross-sectional view among Fig. 1 (hypomere divides thick desulfurization zone and smart desulfurization zone, air-flow centripetal flow).
Among the figure: the 1-adsorptive reactor; The intersegmental front particle blanking pipe of 2-; The intersegmental rear particle blanking pipe of 3-; The intersegmental gas flow tube of 4-; The 5-ammonia sprays into pipe; The 6-check valve; The 7-smoke air inlet; The 8-reactor wall; 9-hypomere annular airflow runner; The outer Johnson Net of 10-; The outer grid of 11-; Activated coke stratum granulosum before the 12-; Johnson Net among the 13-; Grid among the 14-; Activated coke stratum granulosum behind the 15-; Johnson Net in the 16-; The 17-center tube wall; 18/18 '-the central tube mass flow pathway; 19/19 '/19 ' '-particulate material block plate; 20-humidifying cooling nozzle; 21-sieves pipe; The 22-vibratory sieve; 23-annular airflow road (endless tube); The 24-dividing plate; The 25-central tube is strengthened bracing frame; 26-epimere annular airflow mass flow pathway; The 27-exhanst gas outlet; 28-central tube supporting seat; 29-particulate charge pipe; 30-particle discharge pipe.
The specific embodiment
The adsorptive reactor 1 that the utility model Bian uses is radially cross-flow moving bed for the two Π profile shafts of the two sections of combined type, epimere denitration district and hypomere desulfurization zone place in the described reactor wall 8, and by dividing plate 24 upper and lower being separated, the desulfurization of hypomere desulfurization zone is that master, epimere denitration district's denitration are main, realizes SO
2And NO
xUnite and remove.Be characterised in that: described hypomere desulfurization zone ecto-entad is equipped with hypomere annular airflow runner 9, front activated coke stratum granulosum 12, rear activated coke stratum granulosum 15, center tube wall 17 and central tube mass flow pathway 18; The built-in activated coke stratum granulosum in described epimere denitration district communicates with front activated coke stratum granulosum 12 in the hypomere desulfurization zone by intersegmental front particle blanking pipe 2, communicates with described rear activated coke stratum granulosum 15 by intersegmental rear particle blanking pipe 3; The front activated coke stratum granulosum 12 that described hypomere desulfurization zone is built-in and rear activated coke stratum granulosum 15 tops, the below of described dividing plate 24, reactor wall 8 sides from up to down are equipped with gas approach 7 and a plurality of humidifying cooling nozzle 20 successively; The top of activated coke stratum granulosum below, described epimere denitration district, described dividing plate 24, described reactor wall 8 from up to down is equipped with successively exhanst gas outlet 27 and ammonia and sprays into pipe 5; Described gas approach 7 quantity have two, be twoport annular airflow road 23 structures that liquidate, a plurality of smoke gas flows that flue gas is equipped with on annular airflow road 23 outflow of portalling, top, annular airflow road is dividing plate 24, epimere denitration district and hypomere desulfurization zone are separated, prevent from that air-flow from altering to walk to epimere denitration district.So flue gas can only enter hypomere annular airflow runner 9, do centripetal motion by activated coke stratum granulosum 15 behind the front activated coke stratum granulosum 12 of outer shroud and the interior ring, carry out flue gas desulfurization; The epimere ammonia sprays into the NH that pipe 5 radial symmetric spray into
3With the axial flue gas generation local turbulence through making progress from central tube mass flow pathway 18 after the first paragraph cleaning and desulfurization, increase the flue gas mixability, the rear flue gas of mixing is made centrifugal flow and is carried out denitration through epimere activated coke stratum granulosum, then flows out from exhanst gas outlet 27 by epimere annular airflow mass flow pathway 26.During the activated coke desulfurization denitration, the control temperature is 80～130 ℃, air speed 300～500h
-1
Activated coke enters in the adsorptive reactor from the particulate charge pipe at adsorptive reactor top, is introduced into the epimere in the adsorptive reactor, and is slowly mobile downwards under Action of Gravity Field, removes the NO in the flue gas
x, a small amount of sulphur ammonium salt of generation can increase mobile viscous force in activated coke; Activated coke falls into respectively front activated coke stratum granulosum and the rear activated coke stratum granulosum of adsorptive reactor hypomere through intersegmental particle blanking pipe, mainly realizes SO in the flue gas
2Remove; The saturated activated coke of absorption continues to move down under action of gravitation after the desulfurization, discharges adsorptive reactor through the particle discharge pipe, enters follow-up induction system and is transported to the desorption and regeneration tower and regenerate.
Between the intersegmental gas flow tube of adsorptive reactor and activated coke layer, because remaining SO
2With NH
3Reaction, can generate a small amount of ammonium sulfate, cleaning inner member or manhole are set in device, regularly clear up, and establish vibratory sieve at the adsorptive reactor hypomere, when separating broken activated coke and coke powder, also sieve out a part of ammonium sulfate, by above-described method ammonium sulfate is removed, reduce the viscous force in the activated coke motion.
Embodiment
The design gas cleaning of this example and sulfur recovery system can be used for the ultra supercritical fossil-fired unit of unit group 1000MW in the coal-burning power plant, the desulphurization denitration filed of flue gas purification of 600 square metres large-scale smelting sintering machines, large coal-fired boiler or other nonferrous metallurgy tail gas.Design smoke treatment amount 3.0 * 10
6m
3/ h adopts according to circumstances 1 adsorptive reactor list tower processing or adopts a plurality of adsorptive reactor parallel connections to process, design flue gas air speed 300～500h
-1SO in the flue gas composition
2Volume fraction is 1000～4000 * 10
-6, NO
xVolume fraction is 200～800 * 10
-6, also contain part toxic heavy metal ionic mercury, cadmium etc., harmful flue dust.Adsorption temp is at 80～130 ℃; Used adsoption catalyst is qualified, the economical and practical column desulphurization denitration activated coke of performance.By adsorptive reactor, remove the SO in the flue gas
2, NO
x, mercury is with pollutants such as bioxin, realize in an adsorptive reactor, uniting of multi-pollutant being removed.
Design two kinds of operating modes: operating mode 1 is flue gas air speed 300h
-1, operating mode 2 is flue gas air speed 450h
-1, adsorption temp, desorption temperature, design parameter and activated coke loadings are all same with embodiment at this moment; But the activated coke loadings increases by 1.5 times in operating mode 2 adsorptive reactors, and the adsorptive reactor volume increases by 1.5 times, or in two adsorptive reactors that are equivalent to 0.75 times of former adsorptive reactor volume Combined Treatment.
Flue gas from the emission source discharge, behind chimney and air-introduced machine, carry out according to circumstances humidification or adjust temperature, be lower than 2% such as steam volume fraction in the flue gas, then by humidifying cooling nozzle 20 the steam volume fraction in the flue gas is increased to 2～10% scope, temperature controlled to 80～130 ℃ temperature range through overregulating, enter adsorptive reactor;
Flue gas enters in the adsorptive reactor by two smoke inlets that liquidate, and a plurality of smoke gas flows that are equipped with on annular airflow road 23 outflow of portalling realizes the uniform target of ejection; The flue gas that flows out is because stopped by dividing plate 24 above the annular airflow road, can only enter hypomere annular airflow runner 9, do centripetal motion by the front activated coke stratum granulosum 12 of outer shroud and rear activated coke stratum granulosum 15, be introduced into front activated coke layer, in flue gas, there is under the condition and suitable temperature and air speed condition of steam and oxygen the SO in the flue gas
2Catalytic oxidation occurs, and the sulfuric acid that generates ADSORPTION STATE is attached in the micropore of activated coke SO
2Be removed; Flue gas further passes through all the other inner members, enters rear activated coke layer, carries out essence and takes off SO
2Further removed; Flow into the central tube mass flow pathway 18 of hypomere through the flue gas of hypomere purification, flow central tube mass flow pathway 18 interior further making progress, with the NH that sprays into from ammonia ascending pipe 5
3Mix in intersegmental gas flow tube 4, continue upwards to flow into epimere central tube mass flow pathway 18 ', the centrifugal shaft Radial Flow is through activated coke layer, NO in the flue gas
xUnder the catalytic action of activated coke, with NH
3Reaction generates N
2And H
2O, the NO in the flue gas
xBe removed the SO of the one-step removal remnants that go forward side by side
2With other pollutants such as mercury, bioxin, the flue gas after the purification compiles after dirty from epimere annular airflow mass flow pathway 26, flows out through exhanst gas outlet 27, through smoke induced draught fan, enters atmosphere; Desulfurization degree, denitration rate and demercuration rate and Tuo bioxin rate, relevant from the kind of the activated coke of different operating mode, operating condition and use, adopt the utility model activated coke desulfurization denitration diameter of axle to cross-flow moving bed adsorptive reactor, desired value is that desulfurization degree is not less than 95%, the denitration rate is not less than 70%, and demercuration rate and Tuo bioxin rate are not less than 90%.
Above description to the specific embodiment; be intended to the technical scheme that illustrates that the utility model relates to; disclose best implementation method; make those skilled in the art can understand better and implement the utility model; be not be used to limiting protection domain of the present utility model; every based on enlightenment of the present utility model, any apparent equivalent transformation of doing or alternative all should be considered to fall into protection domain of the present utility model.
Claims (6)
1. an activated coke desulfurization denitration diameter of axle is to cross-flow moving bed adsorptive reactor, comprise and placing in the described reactor wall (8), and by on the dividing plate (24), the epimere denitration district of lower separation and hypomere desulfurization zone is characterized in that: described hypomere desulfurization zone ecto-entad is equipped with hypomere annular airflow runner (9) successively, outer Johnson Net (10), outer grid (11), front activated coke stratum granulosum (12), middle Johnson Net (13), middle grid (14), rear activated coke stratum granulosum (15), interior Johnson Net (16), center tube wall (17), central tube mass flow pathway (18); The activated coke stratum granulosum that described epimere denitration district is built-in communicates with front activated coke stratum granulosum (12) in the hypomere desulfurization zone by intersegmental front particle blanking pipe (2), communicates with described rear activated coke stratum granulosum (15) by intersegmental rear particle blanking pipe (3);
The front activated coke stratum granulosum (12) that described hypomere desulfurization zone is built-in and rear activated coke stratum granulosum (15) top, the below of described dividing plate (24) from up to down is equipped with gas approach (7) and a plurality of humidifying cooling nozzle (20) successively on the described reactor wall (8); The top of activated coke stratum granulosum below, described epimere denitration district, described dividing plate (24), described reactor wall (8) from up to down is equipped with successively exhanst gas outlet (27) and ammonia sprays into pipe (5).
According to claim 1 described a kind of activated coke desulfurization denitration diameter of axle to cross-flow moving bed adsorptive reactor, it is characterized in that: described gas approach (7) quantity has two, be twoport annular airflow road (23) structure that liquidates, be equipped with a plurality of smoke gas flows on annular airflow road (23) and portal.
According to claim 1 described a kind of activated coke desulfurization denitration diameter of axle to cross-flow moving bed adsorptive reactor, it is characterized in that: it is 2～4 that described ammonia sprays into pipe (5) quantity, be distributed on the same aspect periphery of described reactor wall (8), ammonia sprays into pipe (5) and is connected with intersegmental gas flow tube (4) by check valve (6) and communicates.
4. described a kind of activated coke desulfurization denitration diameter of axle is characterized in that to cross-flow moving bed adsorptive reactor according to claim 1: described humidifying cooling nozzle (20) quantity is 4～8, the uniform same aspect periphery that is arranged in reactor wall (8).
According to claim 1 described a kind of activated coke desulfurization denitration diameter of axle to cross-flow moving bed adsorptive reactor, it is characterized in that: the upper end of described middle Johnson Net (13) and center tube wall (17) is equipped with respectively axially annular granule material block plate (19/19 ') different in size, and the length of the interior ring particulate material block plate (19) that the upper end of described center tube wall (17) is equipped with is greater than the length of the outer shroud particulate material block plate (19 ') that is equipped with on the described middle Johnson Net (13).
6. described a kind of activated coke desulfurization denitration diameter of axle is characterized in that to cross-flow moving bed adsorptive reactor according to claim 1: the built-in activated coke stratum granulosum in described epimere denitration district is the outside at two ends up and down, is equipped with annular granule material block plate (19 ' ').
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| CN2012204872462U CN202762307U (en) | 2012-09-24 | 2012-09-24 | Axial and radial cross-flow moving bed type adsorption reactor for smoke desulphurization and denitration utilizing activated coke |
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| CN2012204872462U CN202762307U (en) | 2012-09-24 | 2012-09-24 | Axial and radial cross-flow moving bed type adsorption reactor for smoke desulphurization and denitration utilizing activated coke |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102824846A (en) * | 2012-09-24 | 2012-12-19 | 上海龙净环保科技工程有限公司 | Axial and radial cross flow moving bed reactor and activated coke flue gas desulfurization and denitration technology thereof |
| CN105126607A (en) * | 2015-07-31 | 2015-12-09 | 湘潭大学 | Denitration method and device of catalytic cracking regenerated flue gas |
| CN105749741A (en) * | 2016-04-27 | 2016-07-13 | 山西普泰信环保工程有限公司 | Smoke denitration tower |
| CN105771536A (en) * | 2016-03-11 | 2016-07-20 | 神华集团有限责任公司 | Gas adsorption device |
| CN106039926A (en) * | 2016-07-18 | 2016-10-26 | 重集团大连工程建设有限公司 | Flue gas low-resistance desulfurization and denitrification device and desulfurization and denitrification method |
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2012
- 2012-09-24 CN CN2012204872462U patent/CN202762307U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102824846A (en) * | 2012-09-24 | 2012-12-19 | 上海龙净环保科技工程有限公司 | Axial and radial cross flow moving bed reactor and activated coke flue gas desulfurization and denitration technology thereof |
| CN105126607A (en) * | 2015-07-31 | 2015-12-09 | 湘潭大学 | Denitration method and device of catalytic cracking regenerated flue gas |
| CN105126607B (en) * | 2015-07-31 | 2018-08-31 | 湘潭大学 | A kind of method of denitration and device of regeneration fume from catalytic cracking |
| CN105771536A (en) * | 2016-03-11 | 2016-07-20 | 神华集团有限责任公司 | Gas adsorption device |
| CN105749741A (en) * | 2016-04-27 | 2016-07-13 | 山西普泰信环保工程有限公司 | Smoke denitration tower |
| CN106039926A (en) * | 2016-07-18 | 2016-10-26 | 重集团大连工程建设有限公司 | Flue gas low-resistance desulfurization and denitrification device and desulfurization and denitrification method |
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