CN102179130A - Circulating flue gas desulfurization device with fixed bed - Google Patents
Circulating flue gas desulfurization device with fixed bed Download PDFInfo
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 239000003546 flue gas Substances 0.000 title claims abstract description 45
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 24
- 230000023556 desulfurization Effects 0.000 title abstract description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 71
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 51
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000003860 storage Methods 0.000 claims abstract description 8
- 238000001179 sorption measurement Methods 0.000 claims description 39
- 239000007789 gas Substances 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 6
- 239000003517 fume Substances 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 239000008187 granular material Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 28
- 238000004458 analytical method Methods 0.000 abstract description 11
- 238000001035 drying Methods 0.000 abstract description 10
- 238000000638 solvent extraction Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 43
- 230000008569 process Effects 0.000 description 20
- 238000005516 engineering process Methods 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 8
- 239000003610 charcoal Substances 0.000 description 7
- 239000007921 spray Substances 0.000 description 7
- 238000002309 gasification Methods 0.000 description 6
- 230000008859 change Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000009792 diffusion process Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000010410 layer Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000002156 adsorbate Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000005325 percolation Methods 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
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Abstract
The invention discloses a flue gas desulfurization device with a fixed bed, comprising an inner round barrel and an outer round barrel which are mutually and coaxially embedded, wherein the inner round barrel is arranged in the outer round barrel; the top part and the bottom part of the inner round barrel are symmetrically provided with pore-opening round plates; the inner space of the inner round barrel is divided into an analysis area, an absorption area and a drying area along the axial direction of the inner barrel by baffles; the top part and the bottom part of the outer round barrel are respectively provided with partitioning plates corresponding to the positions of the baffles along the arrangement direction of the baffles in the inner barrel; the top part and the bottom part of the outer round barrel are provided with a sector-shaped barrel cover and a sector-shaped water storage plate along the direction of the analysis area, the sector-shaped barrel cover is provided with a nozzle and a circulating water inlet pipe, and the sector-shaped water storage plate is connected with a circulating water outlet pipe; the absorption area is communicated with an inlet and an outlet of a flue gas pipe along the bottom parts of the inner round barrel and the outer round barrel; and the drying area is communicated with a hot air pipe inlet and a hot air pipe outlet along the bottom parts of the inner round barrel and the outer round barrel. In the flue gas desulfurization device, the structure is simple, and three operating steps namely absorption, analysis and drying in active carbon desulfurization can be effectively and synchronously carried out.
Description
Technical field
The present invention relates to a kind of metallurgical and boiler smoke be carried out purification treatment technology, be specifically related to a kind of fixed bed flue gas desulfur device.
Background technology
In recent years, along with the formulation of sustainable development target, the theme of environmental protection is more put on agenda, and along with the strictness day by day of national environmental protection policy, flue gas desulfurization has become the significant problem that China's industry needs to be resolved hurrily at earlier 2000s.Yet because the restriction of economic strength, so far, China mainly is some complete production lines from external introduction, also seldom has the technology maturation that adopts oneself to be applied to the sulfur removal technology of industry.
Existing available desulfur technology is according to control SO
2The position of technology in the coal burning process of discharging can be divided into desulfur technology preceding, back three kinds of the neutralization burning of burning of burning.Desulfurization mainly is coal separation, coal gasification, liquefaction and COAL-WATER SLURRY TECHNOLOGY before the burning; Desulfurization refers to combustion with reduced pollutants, moulded coal and fluidized bed combustion in the burning; Burning back desulfurization also is so-called flue gas desulfurization technique.
Countries in the world research and development and the commercial flue gas desulfurization technique of using are estimated above 200 kinds.Whether reclaim by desulfurization product, flue gas desulfurization, the former directly discharges by the desulfurization mixture if can be divided into the method for abandoning and regeneration absorption method, the latter reclaims desulfurizing byproduct with forms such as sulfuric acid or sulphur.Press the wet form of doing of desulfurization product, flue gas desulfurization can be divided into wet method, semidry method and dry process again.
Activated carbon method flue gas desulfurization be a kind of with absorption effect of mass transmitting be the sulfur method of principle.The selection characterization of adsorption and the catalytic oxidation characteristic of this poromerics of this technology utilization active carbon are to the SO in the flue gas
2Purify up hill and dale and reclaim.Yet still there are many shortcomings in existing activated carbon method flue gas desulfurization technique, as single level system, referring to Fig. 1.This active carbon bed is divided into 4 zonules that area is identical with dividing plate, and for each zonule, sweetening process is mainly by adsorbing and resolving two stages and form.Absorption phase, flue gas flow from bottom to top, when passing active carbon layer, and part SO in the flue gas
2Be adsorbed, flue gas after being purified is sent into chimney by air-introduced machine; Resolution phase, washings are taken away the sulfuric acid of generation by top spray down when passing active carbon layer, washings flow in the neutralization pond and after recycle.
Adopt the shortcoming of existing active carbon desulfurization fixed bed mode mainly to show the following aspects at present:
Absorption and desorb can not be carried out synchronously, cause that equipment is huge, operational management is complicated; Initial cost cost costliness, operating cost is higher; And be not divided into processes such as absorption, parsing, drying, make the activated carbon granule thing of bed easily by coverings such as moisture films, reduced the specific area of particle greatly, reduced absorption property, for example Fig. 2 has provided the change curve of charcoal absorption amount with the active carbon moisture content.As can be seen from the figure when water content was less, active carbon was to SO
2Adsorption capacity reduce along with the increase of water content, this is that the moisture film of formation has reduced the specific area of active carbon because along with the increase of water content, activated carbon surface is wetting gradually.
At the deficiency on the art methods, the invention provides a kind of desulfurization new technology that can move continuously, manage simply and be rich in actual effect.
Summary of the invention
For the technological deficiency that overcomes the above-mentioned background technology is alive not enough, the invention provides a kind of employing absorbent charcoal material to SO
2Gas carries out the inner loop desulfurization fixed bed of continuous adsorption, desorb, drying, earlier with SO
2Be adsorbed on the active carbon, pass through resolving again, make the active carbon desorption, and with the SO of absorption
2Be absorbed into H by water
2SO
4, reach environmental protection and the dual purpose that reclaims useful resources.
In order to realize above-mentioned technical assignment, the present invention adopts following technical scheme to be achieved:
A kind of fixed bed flue gas desulfur device, comprise mutually nested coaxial inner cylindrical and outer cylinder, described inner cylinder places among the outer cylinder, the inner cylinder top and bottom is arranged with the perforate plectane, and inner cylinder inside axially is divided into its inner cylinder inner space three separate districts by baffle plate along inner core; Described outer cylinder top and bottom is respectively equipped with dividing plate along the correspondence position that the inner core baffle plate is provided with direction, outer cylinder inner space also correspondence is divided into resolves district, adsorption zone and dry section; The cylinder top and bottom is provided with fan-shaped cover and fan-shaped water storage plate along resolving district's direction outside, covers at sector drum shower nozzle to be installed and to be recycled into water pipe, is connected with recycling outlet on fan-shaped water storage plate; Adsorption zone is connected with the fume pipe import and export along inner cylinder and outer cylinder bottom; Dry section communicates with the warm-air pipe import and export along inner cylinder and outer cylinder bottom.
Other technologies characteristics of the present invention are: described inner cylinder is an active carbon bed.
Fume pipe described and that adsorption zone and dry section are connected links to each other with heat exchanger respectively with warm-air pipe.
Described inner cylinder and outer cylinder are by the turning cylinder realization coaxial rotation that is connected.
Described perforate plectane passes through gas, water or other fluid, but can not pass through the activated carbon granule thing.
The present invention is different with existing dry method fixed bed desulfurizer is that active carbon bed is divided into three districts is adsorption zone, resolve district, dry section, and three districts independently carry out work synchronously, and assurance utilizes dry activated carbon to SO
2Adsorb.When the adsorption zone active carbon reach saturated after, inner cylinder rotates, and makes the active carbon be in absorption work originally rotate to resolve the district to resolve; Originally the active carbon that was in resolved duty rotates to dry section and carries out drying; Originally the active carbon that was in the duty that is dried rotates to adsorption zone and carries out absorption work.So constantly periodic duty, thus realize absorption, resolve, dry three kinds of operating procedures carry out synchronously.
In addition, utilize heat exchanger to carry out preheating to feeding the dry section air, the temperature of the hot blast of raising helps the drying of dry section active carbon; Utilize heat exchanger to lower the temperature, help the adsorption process of active carbon, because active carbon is to SO to feeding the flue gas of resolving the district
2The absorption of gas belongs to exothermic reaction, reduces the temperature be adsorbed flue gas and helps adsorption process and carry out, and helps also preventing that the specific area owing to exotherm causes the active carbon coking from reducing simultaneously.Because the active carbon moisture content reduces greatly after super-dry, the charcoal absorption amount that provides according to Fig. 2 is with the change curve of active carbon moisture content, and its adsorption efficiency can improve as can be known.
Description of drawings
Fig. 1 is the single level system of existing activated carbon method flue gas desulfurization technique, wherein each icon represent 1 respectively, magnetic valve, 2, washing nozzle, 2, activated carbon bed, 4, gas approach, 5, neutralization pond, 6, clear water reserviors, 7, water circulating pump, 8, exhanst gas outlet.
Fig. 2 charcoal absorption amount is with the change curve of active carbon moisture content.
Fig. 3 is a structural representation of the present invention.
Fig. 4 is a urceolus upward view of the present invention.
Fig. 5 is an inner tube structure schematic diagram of the present invention.
Fig. 6 is flue gas of the present invention and air heat-exchanging device figure.
Fig. 7 is an active carbon desulfurization adsorption process schematic diagram under the hygrometric state.
Below in conjunction with accompanying drawing particular content of the present invention is described in further detail.
The specific embodiment
Referring to Fig. 3-Fig. 6 a kind of fixed bed flue gas desulfur device of the present invention, comprise mutually nested coaxial inner cylindrical 3 and outer cylinder 2, inner cylinder 3 places among the outer cylinder 2, and inner cylinder 3 is an active carbon bed, places absorbent charcoal material.Inner cylinder 3 and outer cylinder 2 are by the turning cylinder 9 realization coaxial rotation that is connected.Inner cylinder 3 top and bottoms are arranged with perforate plectane 8, and inner cylinder 3 inside axially are divided into three separate districts with its inner cylinder 3 inner spaces by baffle plate 7 along inner core; Described outer cylinder 2 top and bottoms are respectively equipped with dividing plate 4 along the correspondence position that inner core 3 interior panellings 7 are provided with direction, outer cylinder 2 inner spaces also correspondence are divided into resolve district I, adsorption zone II and dry section III; Be provided with fan-shaped cover 10 and fan-shaped water storage plate 11 at outer cylinder 2 top and bottoms along resolving district's I direction, shower nozzle 5 be installed on fan-shaped cover 10 and be recycled into water pipe 6, on fan-shaped water storage plate 11, be connected with recycling outlet 1; The adsorption zone II is connected with the fume pipe import and export along inner cylinder 3 and outer cylinder 2 bottoms.The dry section III communicates with the warm-air pipe import and export along inner cylinder 3 and outer cylinder (2) bottom.
In addition, the fume pipe that is connected with adsorption zone (II) and dry section (III) of the present invention links to each other with heat exchanger respectively with warm-air pipe.Utilize heat exchanger to carry out preheating to feeding the dry section air, the temperature of the hot blast of raising helps the drying of dry section active carbon; Utilize heat exchanger to lower the temperature, help the adsorption process of active carbon, because active carbon is to SO to feeding the flue gas of resolving the district
2The absorption of gas belongs to exothermic reaction, reduces the temperature be adsorbed flue gas and helps adsorption process and carry out, and helps also preventing that the specific area owing to exotherm causes the active carbon coking from reducing simultaneously.
Of the present invention active carbon bed is divided into three districts is adsorption zone, resolve district, dry section, three districts carry out work synchronously, when the adsorption zone active carbon reach saturated after, inner cylinder rotates, and makes the active carbon be in absorption work originally rotate to resolve the district to resolve; Originally the active carbon that was in resolved duty rotates to dry section and carries out drying; Originally the active carbon that was in the duty that is dried rotates to adsorption zone and carries out absorption work.The active carbon layer by desorption zone from top to down when the recirculated water of adsorption zone is with the product H of absorption
2SO
4Wash-out comes out, and enters the dilute sulfuric acid pond, when sulfuric acid concentration in the pond reaches 20% left and right sides, changes the shower water in the dilute sulfuric acid pond again.So constantly periodic duty, thus realize absorption, resolve, dry three kinds of operating procedures carry out synchronously.
Below provide relative theory analysis of the present invention and checking computational process:
The method that fixed bed flue gas desulfur device of the present invention specifically adopts the nozzle spray to resolve, the inventor is analyzed according at present existing 4 kinds of different analytic methods:
Method I: after adsorption process finishes, adsorption column air inlet and water discharging valve are closed simultaneously, 1000ml distilled water is injected adsorption column active carbon is carried out the immersion of 3min, when soaking, use agitator that active carbon is stirred.
The method II: process is with the method I, but do not add whipping process.
The method III: highly locating to be provided with the aperture apart from bed 0.5m in adsorption column is that 0.2mm, thickness are the stainless steel orifice plate of 50mm, and adsorption process is closed intake valve after finishing, and the opening water discharge valve evenly drenched adsorption column with 1000ml distilled water in 3 minutes.
The method IV: highly locate to install 1/2''PZ5095 * 45J type nozzle and supply water with circulating pump apart from bed 0.5m in adsorption column, water-washing process is with the method III.
Four kinds of methods analyzing efficiency in suction-parse cycle for the first time sees Table 1.
As shown in Table 1, the analytic method of soaking and stirring has the highest analyzing efficiency, this is because stirring action makes absorbent particles be contacted fully with fluid, and under the high speed turning effort, the turbulence effect that fluid produces obviously strengthens the diffusion of adsorbate in fluid, mass tranfer coefficient increases greatly, thereby can more fully resolve.And the minimum reason of static immersing analyzing efficiency is: under the fluid inactive state, and the H of ADSORPTION STATE
2SO
4The power that molecule can only rely on dissolution to produce is separated from adsorbent, along with H near the solution adsorbent surface layer
2SO
4Molecule intensive, this diffusion weakens gradually, when diffusion power during with the diffusional resistance balance, promptly can not continue parsing.
The new active carbon of MHY30 type is inhaled-analyzing efficiency of parse cycle for the first time under the different analytic methods of table 1
（m
ac=1.5kg，V
SO2=3.0×10
-3，V
H2O=0.1，T=80℃，W
de=1L，t
de=3min）
Yet in the real practical application, the method for immersion also is difficult to be applied to successional industrial production, and the water spray type analytic method is a kind of relatively actual analytic method.In two kinds of water spray type analytic methods, the parsing amount that the nozzle spray is resolved is slightly larger than orifice plate trickle parsing amount.This mainly is that percolation flow velocity has certain difference in two kinds of analytic methods because under the identical situation of trickle amount.In the orifice plate trickle process, because current only depend on the gravity effect dirty naturally, orifice plate has bigger local flow resistance again, makes the initial velocity of current very low.And in the nozzle spray, owing to have certain pressure head, water outlet has certain speed, and 1/2''PZ5095 * 45J type nozzle that this experiment is adopted under the pressure of 0.1Mpa, goes out water speed and is about 2.41m/s.Therefore, through experimental studies have found that, when the trickle height is all 0.5m, the percolation flow velocity when adopting the nozzle spray to resolve is about the orifice plate trickle when resolving 1.5 ~ 2.0 times.
In addition, the active carbon desulfurization adsorption process is as shown in Figure 7 under the existing hygrometric state.Sulfur dioxide is to remove from flue gas by physical absorption and chemisorbed dual mode under the as can be seen from the figure existing hygrometric state.For the allovitalism charcoal, the SO of active carbon under the hygrometric state
2The intragranular diffusion coefficient is less than the active carbon under the anhydrous condition, thereby proved that further active carbon is to SO under the water condition
2Absorption be a kind of chemisorbed, it has slower adsorption rate.
Yet active carbon is to rely on inter-molecular attraction that adsorbate is adsorbed on the physical absorption that adsorbent shows to the absorption of sulfur dioxide fully under the dry state, itself and present stage the active carbon flue gas desulfurizing theory have essential distinction.For realize adsorbing, the continuity of parsing, dry run, the special workspace of making three cycle rotations of the present invention.And utilize the flue gas of discharging by economizer, and the air that dry run is needed carries out preheating earlier, and one side has reduced the temperature of flue gas itself, promotes adsorption process to carry out smoothly, because absorption is exothermic process, reduces flue-gas temperature and helps the adsorption process generation.Solve the hot blast of the required acquisition of dry run on the other hand, saved the needed energy of heating hot blast.
In order to verify that heat exchange can obtain to heat the hot blast energy needed to fixed bed flue gas desulfur device of the present invention through heat exchanger, the spy has carried out following calculating and has been verified:
The flue gas that feeds the fixed bed flue gas desulfur device is through temperature t behind the economizer
1Be 160 ℃, the concentration C of sulfur dioxide in flue gas
1Be 4500 mg/m
3, exhanst gas outlet concentration is coal-burning boiler II period national standard C
2Be 900mg/m
3, promptly desulfuration efficiency 80%, and flue gas flow L is 36000m
3/ h.Because active carbon is stabilizing to 25 ℃, pressure is that the equilibrium adsorption capacity S under the 100kpa is 10%, so required quality of activated carbon is:
In order to make the active carbon dry run carry out smoothly, need to carry out preheating through heat exchanger and obtain hot blast air, preheating institute calorific requirement is flowed through by flue gas and air, and heat exchange obtains behind the heat exchanger.Before the preheating, air themperature t
2Be 20 ℃ of normal temperature, the air themperature t after preheating
3Be 50 ± 5 ℃, relative humidity d
1Be 10%, flue-gas temperature t after lowering the temperature
4Be 60 ± 5 ℃, the utilization countercurrent action is carried out heat exchange.The required gasification latent heat of evaporation water steam is provided by the hot-air that flows through dry section in the dry run, the hot-blast outlet temperature t
5Be 10 ℃, relative humidity d
2Be 100%.According to the heat balance principle:
,
In the formula:
---the required gasification latent heat that provides of dry run, KJ/kg;
The required gasification latent heat that provides of dry run is:
In the formula:
---the quality of institute's evaporation water steam, kg;
In order to guarantee the adsorbance of adsorption process, according to the change curve of charcoal absorption amount with the active carbon moisture content, thus need to make the dried active carbon moisture content of process less than 5%, and the calculating of present embodiment reality is taken as 0.Active carbon moisture content after resolving is 50%, then per hour needs the quality of transpiring moisture to be
Kg, i.e. 648kg, evaporating required gasification latent heat Q is 1644624KJ, establishing dry run heat transfer efficiency k is 50%, so the hot blast rate that per hour needs to feed is
Kg/h.Because the density of air
Be 1.293kg/m
3So, be roughly equal to 62289.1m3/h.If flue-gas temperature is the same with air enthalpy, then the heat exchange efficiency of required heat exchanger is,
, and actual engineering can satisfy such heat exchange efficiency fully, visible dry run institute energy requirement can be obtained by flue gas and hot blast heat exchange fully.
Claims (5)
1. fixed bed flue gas desulfur device, it is characterized in that: comprise mutually nested coaxial inner cylindrical (3) and outer cylinder (2), described inner cylinder (3) places among the outer cylinder (2), inner cylinder (3) top and bottom is arranged with perforate plectane (8), and inner cylinder (3) is inner axially to be divided into three separate workspaces with its inner cylinder (3) inner space by baffle plate (7) along inner core; Described outer cylinder (2) top and bottom is respectively equipped with dividing plate (4) along the correspondence position that inner core (3) interior panelling (7) is provided with direction, outer cylinder (2) inner space also correspondence is divided into resolves district (I), adsorption zone (II) and dry section (III); Be provided with fan-shaped cover (10) and fan-shaped water storage plate (11) at outer cylinder (2) top and bottom along resolving district's (I) direction, shower nozzle (5) is installed on fan-shaped cover (10) and is recycled into water pipe (6), on fan-shaped water storage plate (11), be connected with recycling outlet (1); Adsorption zone (II) is connected with the fume pipe import and export along inner cylinder (3) and outer cylinder (2) bottom; Dry section (III) communicates with the warm-air pipe import and export along inner cylinder (3) and outer cylinder (2) bottom.
2. fixed bed flue gas desulfur device as claimed in claim 1 is characterized in that: described inner cylinder (3) is an active carbon bed.
3. fixed bed flue gas desulfur device as claimed in claim 1 is characterized in that: the described fume pipe that is connected with adsorption zone (II) and dry section (III) links to each other with heat exchanger respectively with warm-air pipe.
4. fixed bed flue gas desulfur device as claimed in claim 1 is characterized in that: described inner cylinder (3) and outer cylinder (2) are by turning cylinder (9) the realization coaxial rotation that is connected.
5. fixed bed flue gas desulfur device as claimed in claim 1 is characterized in that: described perforate plectane (8) can pass through gas or aqueous fluid, and can not pass through the activated carbon granule thing.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102513035A (en) * | 2011-12-15 | 2012-06-27 | 昆明理工大学 | Rotary type continuous feed fixed bed reactor |
| CN104411960A (en) * | 2012-06-01 | 2015-03-11 | 曼柴油机和涡轮机欧洲股份公司 | Internal combustion engine having an exhaust gas supercharging system and an exhaust gas recirculation system |
| CN105854508A (en) * | 2016-04-20 | 2016-08-17 | 河北先河正源环境治理技术有限公司 | Combined type VOCs (Volatile Organic Chemicals) purification and recovery device |
| CN109647132A (en) * | 2018-12-29 | 2019-04-19 | 山东师范大学 | A kind of rotary active carbon flue gas desulfurizing device |
| CN109908698A (en) * | 2018-12-29 | 2019-06-21 | 山东师范大学 | A rotary activated carbon flue gas desulfurization and denitrification device |
| CN115486552A (en) * | 2022-11-07 | 2022-12-20 | 云南中烟工业有限责任公司 | A rotary vacuum dampening device and a dampening method for tobacco materials |
| CN115738692A (en) * | 2022-10-24 | 2023-03-07 | 江苏垦乐节能环保科技有限公司 | Rotary kiln pelletizing flue gas reposition of redundant personnel denitrification facility |
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| US3847572A (en) * | 1971-07-14 | 1974-11-12 | Hitachi Ltd | Apparatus for desulfurizing flue gas |
| CN2902424Y (en) * | 2006-04-17 | 2007-05-23 | 王惠生 | Active carbon desulfur reversal synchronous working tower |
| CN101058051A (en) * | 2006-04-17 | 2007-10-24 | 王惠生 | Active carbon flue gas desulfurizing reverse synchronous work tower |
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Cited By (10)
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| CN102513035A (en) * | 2011-12-15 | 2012-06-27 | 昆明理工大学 | Rotary type continuous feed fixed bed reactor |
| CN102513035B (en) * | 2011-12-15 | 2014-05-07 | 昆明理工大学 | Rotary type continuous feed fixed bed reactor |
| CN104411960A (en) * | 2012-06-01 | 2015-03-11 | 曼柴油机和涡轮机欧洲股份公司 | Internal combustion engine having an exhaust gas supercharging system and an exhaust gas recirculation system |
| CN105854508A (en) * | 2016-04-20 | 2016-08-17 | 河北先河正源环境治理技术有限公司 | Combined type VOCs (Volatile Organic Chemicals) purification and recovery device |
| CN105854508B (en) * | 2016-04-20 | 2018-08-31 | 河北先河正源环境治理技术有限公司 | A kind of combined type VOCs purification recovery devices |
| CN109647132A (en) * | 2018-12-29 | 2019-04-19 | 山东师范大学 | A kind of rotary active carbon flue gas desulfurizing device |
| CN109908698A (en) * | 2018-12-29 | 2019-06-21 | 山东师范大学 | A rotary activated carbon flue gas desulfurization and denitrification device |
| CN115738692A (en) * | 2022-10-24 | 2023-03-07 | 江苏垦乐节能环保科技有限公司 | Rotary kiln pelletizing flue gas reposition of redundant personnel denitrification facility |
| CN115486552A (en) * | 2022-11-07 | 2022-12-20 | 云南中烟工业有限责任公司 | A rotary vacuum dampening device and a dampening method for tobacco materials |
| CN115486552B (en) * | 2022-11-07 | 2024-01-19 | 云南中烟工业有限责任公司 | Rotary vacuum conditioning equipment and conditioning method for tobacco materials |
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