CN203694875U - Radial cross-flow moving-bed reactor for removal of hydrogen sulfide by temperature swing adsorption - Google Patents
Radial cross-flow moving-bed reactor for removal of hydrogen sulfide by temperature swing adsorption Download PDFInfo
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- CN203694875U CN203694875U CN201420087239.2U CN201420087239U CN203694875U CN 203694875 U CN203694875 U CN 203694875U CN 201420087239 U CN201420087239 U CN 201420087239U CN 203694875 U CN203694875 U CN 203694875U
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- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 33
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 239000002245 particle Substances 0.000 claims description 45
- 239000002250 absorbent Substances 0.000 claims description 42
- 230000002745 absorbent Effects 0.000 claims description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 32
- 239000003546 flue gas Substances 0.000 claims description 32
- 238000007599 discharging Methods 0.000 claims description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 230000003647 oxidation Effects 0.000 claims description 11
- 238000007254 oxidation reaction Methods 0.000 claims description 11
- 238000013459 approach Methods 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 10
- 239000003054 catalyst Substances 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 239000000571 coke Substances 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 238000009826 distribution Methods 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000005192 partition Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 15
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 9
- 230000023556 desulfurization Effects 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 230000006872 improvement Effects 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 5
- 239000003610 charcoal Substances 0.000 description 5
- 238000013461 design Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 230000006698 induction Effects 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000037361 pathway Effects 0.000 description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M potassium hydroxide Inorganic materials [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- -1 sulfide hydrogen Chemical class 0.000 description 2
- 206010016173 Fall Diseases 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a radial cross-flow moving-bed reactor for removal of hydrogen sulfide by temperature swing adsorption. The reactor comprises a feeding section, a reaction section and a discharge section sequentially from the top down, wherein a feeding structure of the blanking section ensures uniform blanking; with the adoption of a gas uniformity partition structure of the reaction section, axial and radial uniform inlet gas distribution is ensured, and inlet gas pressure drop is reduced; an annular discharge pipe and a funnel discharge structure of the discharge section ensure uniform feeding and overcome the phenomenon that the moving-down speed of grains in a central area is greater than that of grains on a wall. The reactor can be used for removing much high-concentration gas containing hydrogen sulfide, and has the advantages of uniform feeding, stable continuous operation, and equipment investment and running cost economization.
Description
Technical field
The utility model relates to stack gases process for comprehensively treating field, relates in particular to a kind of Temp .-changing adsorption and remove the radially cross-flow moving bed reactor of hydrogen sulfide.
Background technology
In recent years, in the time that producing the products such as ammonia, methyl alcohol, methanation coal gas as raw material, coal, oil and natural gas mostly use effective catalyst or noble metal catalyst, unstripped gas medium sulphide content is poisoning is the main cause of catalysqt deactivation, and the sulfide of trace comprises hydrogen sulfide (H
2s is 0.1 × 10
-6) just can make catalyst lose activity completely; In addition, sulfide hydrogen (H
2s) after fuel gas burning, generate SO
2, can form acid rain, contaminated environment, very easily corroding metal, blocking pipe etc.Therefore, effectively from unstripped gas and fuel gas, remove hydrogen sulfide (H
2s) in chemical industry, occupy very consequence.
Up to now, sulfur removal technology mainly contains dry desulfurization, wet desulphurization and bioanalysis desulfurization three major types, wherein the Application and Development of wet desulphurization agent is very general, technology is also more ripe, desulfuration efficiency is high, but in waste water last handling process, exist secondary pollution, the problem such as organic matter toxicity is large, equipment is huge, energy consumption is large and cost is high, sulfur recovery and Ta Nei sulphur are stifled.Dry desulfurization mainly comprises absorption method, membrane separation process and low temperature processing etc.Dry desulfurization can overcome the shortcoming of wet desulphurization, and process simplification, easy to operate, equipment is simple, cost is low, it is little to load, and inorganic sulfur and organic sulfur are all had compared with high purification.Meanwhile, when Dry Adsorption removes hydrogen sulfide, can also reclaim the sulphur resource that China needs import, realize the doulbe-sides' victory of economy and environmental protection, become the focus of research at present.
Hydrogen sulfide (H in industry
2s) absorber adopts fixed bed mostly, and multiple switching assurance techniques are moved continuously, and this technique is along with the increase of exhaust gas volumn, and equipment increases, operation control system more sophisticated.Because the restriction of technique causes, the absorption method amount of being generally used for is little, the low (H of concentration
2s content is less than 0.05 × 10
-6) sulfide hydrogen (H
2s) gas.Adopt moving bed can overcome this defect, but current radially moving bed blanking often run into all problems of the yielding damage of depressed structure sector drum of blanking uneven phenomenon, runner.
Therefore, the applicant is devoted to develop a kind of Temp .-changing adsorption for the problems referred to above and removes the radially cross-flow moving bed reactor of hydrogen sulfide, can be used for the sulfide hydrogen (H that the amount of removing is large, concentration is high
2s) gas, and uniform blanking.
Utility model content
In view of the deficiency that above-mentioned prior art exists, the utility model proposes a kind of sulfide hydrogen (H that the amount of removing is large, concentration is high that can be used for
2s) gas, and the Temp .-changing adsorption of uniform blanking removes the radially cross-flow moving bed reactor of hydrogen sulfide.
The utility model is for achieving the above object, a kind of Temp .-changing adsorption that the utility model provides removes the radially cross-flow moving bed reactor of hydrogen sulfide, from top to bottom comprise successively: for inputting the blanking section of absorbent particles, for the conversion zone that flue gas is processed, and for exporting the discharging section of the saturated absorbent particles of absorption.
Described blanking section comprises storage tank, blanking funnel structure and feed pipe.
Described conversion zone is disposed with wall, air inlet layer, outer Johnson Net, absorbent particles layer, interior Johnson Net and central tube from outside to inside, leaves gap and form described air inlet layer between described wall and outer Johnson Net.
Described wall is provided with some vertical chutes on the medial surface of described outer Johnson Net, every described vertical chute is along the medial surface layout extending longitudinally of described wall, on vertical chute every described, plug an equal air bound plate, described air inlet layer is divided into multiple runners, and leaves gap between described equal air bound plate and described outer Johnson Net.
Described discharging section comprises annular discharge nozzle and discharging funnel structure.
As further improvement of the utility model, it is upper that described annular discharge nozzle is arranged in described absorbent particles layer bottom, and collect output by described discharging funnel structure.
As further improvement of the utility model, described conversion zone top is also provided with oxidation air import, humidifying nozzle and two gas approach that arrange in opposite directions, and described oxidation air import and the equal conducting of described humidifying nozzle are connected to described air inlet layer.
As further improvement of the utility model, described feed pipe quantity is 4-8, is evenly plugged on described absorbent particles layer top.
As further improvement of the utility model, the built-in absorbent particles of described absorbent particles layer is active carbon, active carbocoal, modified activated carbon and/or using modified activated semi-coke catalyst.
It is as follows that Temp .-changing adsorption of the present utility model removes the beneficial effect of radially cross-flow moving bed reactor of hydrogen sulfide:
1. effectively realize hydrogen sulfide (H
2removing S);
2. can process larger exhaust gas volumn hydrogen sulfide (H
2removing S);
3. absorbent particles layer uniform blanking, only needs a feed opening control node;
4. runner flue gas even distribution is simple in structure, is difficult for deformed damaged, and radially flue gas even distribution successful, easily processes and install, and also can reduce reactor perforation pressure drop;
5. the design of oxidation air import and layout, flue gas, oxidation air mix, and effectively improve hydrogen sulfide (H
2s) removal efficiency;
6. continuously stable, save equipment investment and operating cost.
Accompanying drawing explanation
Fig. 1 is the structural representation that Temp .-changing adsorption of the present utility model removes the radially cross-flow moving bed reactor of hydrogen sulfide.
Fig. 2 is the A-A cross-sectional view in Fig. 1.
Fig. 3 is the B-B cross-sectional view in Fig. 1.
Fig. 4 is the C-C cross-sectional view in Fig. 1.
Fig. 5 is the D-D cross-sectional view in Fig. 1.
Primary clustering symbol description in figure:
Blanking section 100, storage tank 110, blanking funnel structure 120, feed pipe 130, conversion zone 200, wall 210, vertical chute 211, all air bound plate 212, air inlet layer 220, runner 221, outer Johnson Net 230, absorbent particles layer 240, interior Johnson Net 250, central tube 260, mass flow pathway 261, exhanst gas outlet 262, gas approach 270, oxidation air import 280, humidifying nozzle 290, discharging section 300, annular discharge nozzle 310, discharging funnel structure 320, discharging opening 321.
The specific embodiment
In order to be illustrated more clearly in the utility model embodiment or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only embodiment more of the present utility model, for those of ordinary skills, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
Fig. 1 is the structural representation that Temp .-changing adsorption of the present utility model removes the radially cross-flow moving bed reactor of hydrogen sulfide.As shown in Figure 1, a kind of Temp .-changing adsorption that the present embodiment proposes removes the radially cross-flow moving bed reactor of hydrogen sulfide, from top to bottom comprise successively: for inputting the blanking section 100 of absorbent particles, for the conversion zone 200 that flue gas is processed, and for exporting the discharging section 300 of the saturated absorbent particles of absorption; Blanking section 100 coupled reaction sections 200, conversion zone 200 connects blanking section 100, and blanking section 100 is inputted conversion zone 200 by absorbent particles the flue gas of process is adsorbed, and finally by discharging section 300, the saturated absorbent particles of absorption is exported.
Shown in Fig. 4, conversion zone 200 is disposed with wall 210, air inlet layer 220, outer Johnson Net 230, absorbent particles layer 240, interior Johnson Net 250 and central tube 260 from outside to inside, between wall 210 and outer Johnson Net 230, leave gap and form air inlet layer 220, conversion zone 200 tops are provided with gas approach 270, gas approach 270 conductings are connected to air inlet layer 220, flue gas is entered in air inlet layer 220 by gas approach 270, see through successively outer Johnson Net 230, absorbent particles layer 240 and interior Johnson Net 250, finally enter central tube 260 and export.
As shown in Figure 1 and Figure 4, the wall 210 of the present embodiment is provided with 20 vertical chutes 211 on the medial surface of outer Johnson Net 230, every vertical chute 211 is along the medial surface layout extending longitudinally of wall 210, on every vertical chute 211, plug an equal air bound plate 212, air inlet layer 220 is divided into 20 runners 221, and all between air bound plate 212 and outer Johnson Net 230, leave gap (shown in Figure 4), so that better balance radial gas distributes.
As shown in figures 1 and 3, the gas approach 270 of the present embodiment is two, and two gas approach 270 are to arrange in opposite directions, are the twoport structure that liquidates.In addition, be also provided with oxidation air import 280 and humidifying nozzle 290 on conversion zone 200 tops, oxidation air import 280 and the equal conducting of humidifying nozzle 290 are connected to air inlet layer 220.Exemplary, humidifying nozzle 290 quantity are 2, are 90 ° of intervals and arrange.
As depicted in figs. 1 and 2, the blanking section 100 of the present embodiment comprises storage tank 110, blanking funnel structure 120 and feed pipe 130, and storage tank 110 is connected to absorbent particles layer 240 by blanking funnel structure 120 and feed pipe 130 conductings.Exemplary, feed pipe 130 quantity of the present embodiment are 4, as shown in Figure 2, are evenly plugged on absorbent particles layer 240 top.Wherein, the built-in absorbent particles of absorbent particles layer 240 can select the one or more combination of active carbon, active carbocoal, modified activated carbon and/or using modified activated semi-coke catalyst to use as required, repeats no more herein.
As shown in Figure 1 and Figure 5, the discharging section 300 of the present embodiment comprises annular discharge nozzle 310 and discharging funnel structure 320, annular discharge nozzle 310 is arranged on absorbent particles layer 240 bottom, and collect output by discharging funnel structure 320, discharging opening 321 by discharging funnel structure 320 is exported, and convenience is connected with follow-up device for transporting objects.
Certainly, in other specific embodiments, the concrete structure of blanking section and discharging section can be adjusted according to actual needs, if the quantity of the feed pipe of blanking section can be other quantity such as 5-8 root, repeats no more herein.
Concrete, the Temp .-changing adsorption that the radially cross-flow moving bed reactor that staff can adopt the Temp .-changing adsorption of the present embodiment to remove hydrogen sulfide carries out flue gas processing removes hydrogen sulfide method, comprises the steps:
1) described absorbent particles is interior in feed pipe 130 enters absorbent particles layer 240 from storage tank 110, slowly mobile downwards under Action of Gravity Field, removes the hydrogen sulfide in flue gas; After desulfurization, adsorb saturated absorbent particles and continue to move down under the effect of gravity, discharge through discharging section 300, enter follow-up induction system to regenerator and regenerate, the high-concentration hydrogen sulfide (H that absorbent particles reclaims
2s) can be used for CLAUS device and prepare sulphur.
2) described flue gas enters air inlet layer 220 by gas approach 270, then does centripetal motion by absorbent particles layer, carries out flue gas desulfurization, and flue gas desulfurization collects output from central tube 260 after purifying.
Concrete, absorbent particles can be selected active carbon, active carbocoal, modified activated carbon and/or using modified activated semi-coke catalyst according to actual conditions.Wherein, modified activated carbon or using modified activated semi-coke catalyst (blue charcoal) can select to flood K
2cO
3, Na
2cO
3, KOH, NaOH, metal and metal oxide etc.
The radially cross-flow moving bed reactor that the Temp .-changing adsorption of the present embodiment removes hydrogen sulfide can be used for the depriving hydrogen sulphide (H of ammonia, methyl alcohol, methanation Gas Production, coal-burning boiler, oil exploitation
2s) filed of flue gas purification.Exemplary, design smoke treatment amount 5.0 × 10
5m
3/ h, optionally adopts 1 reactor list tower to process or adopts multiple reactor parallel connection to process, design flue gas air speed 500～2000h
-1.Hydrogen sulfide (H in flue gas composition
2s) volume fraction is 10～2000 × 10
-6, also contain part toxic heavy metal ionic mercury, cadmium etc., harmful flue dust.Adsorption temp is at 20～200 ℃; Sorbent used particle is qualified, the economical and practical active carbon of performance, active carbocoal (blue charcoal) or the active carbon of modification and the active carbocoal of modification (blue charcoal).By reactor, remove the hydrogen sulfide (H in flue gas
2s), the high-concentration hydrogen sulfide (H of recovery
2s) can be used for CLAUS device and prepare sulphur.
Design two kinds of operating modes: operating mode 1 is flue gas air speed 800h
-1, operating mode 2 is flue gas air speed 1500h
-1, now adsorption temp, design parameter and absorbent particles loadings are all same with embodiment; But absorbent particles loadings increases by 2 times in operating mode 2 reactors, reactor volume increases by 2 times, or in two reactors that are equivalent to 0.9 times of former reactor volume Combined Treatment.
The flue gas of discharging from emission source, after chimney and air-introduced machine, adjusts temperature depending on adsorbent kind, if absorbent particles is active carbon or active carbocoal (blue charcoal), temperature is entered to reactor after overregulating the temperature range that controls to 80～150 ℃; Also need optionally humidification, if steam volume fraction in flue gas is lower than 2%, by humidifying nozzle, the steam volume fraction in flue gas is increased to 2～10% scope; Absorbent particles is active carbon or the using modified activated semi-coke catalyst (blue charcoal) of modification, and temperature is entered to reactor after overregulating the temperature range that controls to 20～100 ℃.
Flue gas enters in conversion zone by two gas approach 270 that liquidate, and if oxygen purity in flue gas is lower than 2%, by oxidation air import 280, the oxygen purity in flue gas is increased to 2～5% scope; After flue gas oxygen mix, enter runner 221 downwards, all air bound plate 212 impels flue gas to flow downward straight, due to equal air bound plate 212 and the gap of outer Johnson Net 230, impels again the different exhaust gas volumns between different dividing plates to carry out again uniform; Afterwards, flue gas, by the centripetal motion of outer Johnson Net 230, enters absorbent particles layer 240, has under the condition and suitable temperature and air speed condition of oxygen the hydrogen sulfide (H in flue gas in flue gas
2s) there is catalytic oxidation, generate elemental sulfur (S) and be attached in the micropore of adsorbent, hydrogen sulfide (H
2s) be removed; Flue gas further passes through all the other inner members, enters in the runner of central tube 260, interior further upwards mobile at the mass flow pathway 261 of central tube 260, discharges from exhanst gas outlet 262, through smoke induced draught fan (not shown), enters atmosphere; Depriving hydrogen sulphide rate is relevant from the kind of the adsorbent of different operating mode, operating condition and use, adopts radially cross-flow moving bed adsorptive reactor and the method for the present embodiment, and desired value is that depriving hydrogen sulphide rate is not less than 95%.Hydrogen sulfide (H
2s) concentration of emission can meet national Specification≤0.02mg/L.
Absorbent particles is interior through four blanking funnel structure 120 free-fallings from storage tank 110, enters in absorbent particles layer 240 through four uniform feed pipes 130, slowly mobile downwards under Action of Gravity Field, removes the hydrogen sulfide (H in flue gas
2s); After desulfurization, adsorb saturated absorbent particles continues to move down under the effect of gravity, by annular discharge nozzle 310 and the blanking funnel structure 120 of absorbent particles layer 240 bottom, discharge through discharging opening 321, enter follow-up induction system and be transported to desorption and regeneration tower and regenerate, the high-concentration hydrogen sulfide (H of recovery
2s) can be used for CLAUS device and prepare sulphur.
Therefore the baiting structure of the present embodiment blanking section has guaranteed uniform blanking; The structure setting of the equal air bound plate of described conversion zone, guarantee Intake shaft to being uniformly distributed radially, and reduce air inlet pressure drop; The annular discharge nozzle of described discharging section and funnel discharging structure, guarantee uniform blanking, overcome center particle and moved down the phenomenon that speed is greater than wall place particle and moves down speed, can be used for the H 2 S-containing gas that the amount of removing is large, concentration is high, there is uniform blanking, continuously stable, the advantage of saving equipment investment and operating cost.
The above is only preferred embodiment of the present utility model; it should be pointed out that for those skilled in the art, do not departing under the prerequisite of the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (5)
1. a Temp .-changing adsorption removes the radially cross-flow moving bed reactor of hydrogen sulfide, it is characterized in that: from top to bottom comprise successively: for inputting the blanking section of absorbent particles, for the conversion zone that flue gas is processed, and for exporting the discharging section of the saturated absorbent particles of absorption;
Described blanking section comprises storage tank, blanking funnel structure and feed pipe;
Described conversion zone is disposed with wall, air inlet layer, outer Johnson Net, absorbent particles layer, interior Johnson Net and central tube from outside to inside, leaves gap and form described air inlet layer between described wall and outer Johnson Net;
Described wall is provided with some vertical chutes on the medial surface of described outer Johnson Net, every described vertical chute is along the medial surface layout extending longitudinally of described wall, on vertical chute every described, plug an equal air bound plate, described air inlet layer is divided into multiple runners, and described equal air bound plate
And leave gap between described outer Johnson Net;
Described discharging section comprises annular discharge nozzle and discharging funnel structure.
2. Temp .-changing adsorption as claimed in claim 1 removes the radially cross-flow moving bed reactor of hydrogen sulfide, it is characterized in that: it is upper that described annular discharge nozzle is arranged in described absorbent particles layer bottom, and collect output by described discharging funnel structure.
3. Temp .-changing adsorption as claimed in claim 1 removes the radially cross-flow moving bed reactor of hydrogen sulfide, it is characterized in that: described conversion zone top is also provided with oxidation air import, humidifying nozzle and two gas approach that arrange in opposite directions, and described oxidation air import and the equal conducting of described humidifying nozzle are connected to described air inlet layer.
4. Temp .-changing adsorption as claimed in claim 1 removes the radially cross-flow moving bed reactor of hydrogen sulfide, it is characterized in that: described feed pipe quantity is 4-8, is evenly plugged on described absorbent particles layer top.
5. Temp .-changing adsorption as claimed in claim 1 removes the radially cross-flow moving bed reactor of hydrogen sulfide, it is characterized in that: the built-in absorbent particles of described absorbent particles layer is active carbon, active carbocoal, modified activated carbon and/or using modified activated semi-coke catalyst.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420087239.2U CN203694875U (en) | 2014-02-27 | 2014-02-27 | Radial cross-flow moving-bed reactor for removal of hydrogen sulfide by temperature swing adsorption |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420087239.2U CN203694875U (en) | 2014-02-27 | 2014-02-27 | Radial cross-flow moving-bed reactor for removal of hydrogen sulfide by temperature swing adsorption |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103768892A (en) * | 2014-02-27 | 2014-05-07 | 上海龙净环保科技工程有限公司 | Radial cross-flow moving bed reactor for adsorbing and removing hydrogen sulfide at variable temperature |
| WO2019091338A1 (en) * | 2017-11-10 | 2019-05-16 | 中冶长天国际工程有限责任公司 | Activated carbon adsorption tower, flue gas purification method, and desulfurization and denitrification system |
-
2014
- 2014-02-27 CN CN201420087239.2U patent/CN203694875U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103768892A (en) * | 2014-02-27 | 2014-05-07 | 上海龙净环保科技工程有限公司 | Radial cross-flow moving bed reactor for adsorbing and removing hydrogen sulfide at variable temperature |
| CN103768892B (en) * | 2014-02-27 | 2015-07-08 | 上海龙净环保科技工程有限公司 | Radial cross-flow moving bed reactor for adsorbing and removing hydrogen sulfide at variable temperature |
| WO2019091338A1 (en) * | 2017-11-10 | 2019-05-16 | 中冶长天国际工程有限责任公司 | Activated carbon adsorption tower, flue gas purification method, and desulfurization and denitrification system |
| CN109772097A (en) * | 2017-11-10 | 2019-05-21 | 中冶长天国际工程有限责任公司 | Activated carbon adsorber and flue gas purifying method |
| CN109772097B (en) * | 2017-11-10 | 2020-07-03 | 中冶长天国际工程有限责任公司 | Activated carbon method flue gas purification device and flue gas purification method |
| RU2746856C1 (en) * | 2017-11-10 | 2021-04-21 | Чжуне Чантянь Интернешнал Энджиниринг Ко., Лтд. | Activated carbon adsorption column, exhaust gas purification process and desulfurization and denitrification system |
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