CN206304563U - SO in a kind of pyrolusite pulp removing flue gas2And its device of recycling - Google Patents
SO in a kind of pyrolusite pulp removing flue gas2And its device of recycling Download PDFInfo
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- CN206304563U CN206304563U CN201621151643.7U CN201621151643U CN206304563U CN 206304563 U CN206304563 U CN 206304563U CN 201621151643 U CN201621151643 U CN 201621151643U CN 206304563 U CN206304563 U CN 206304563U
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- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 238000004064 recycling Methods 0.000 title claims abstract description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000003546 flue gas Substances 0.000 claims abstract description 54
- 239000002002 slurry Substances 0.000 claims abstract description 48
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 35
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 230000023556 desulfurization Effects 0.000 claims abstract description 32
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 28
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 27
- 238000001035 drying Methods 0.000 claims abstract description 25
- 238000000746 purification Methods 0.000 claims abstract description 22
- 238000005352 clarification Methods 0.000 claims abstract description 21
- 238000004062 sedimentation Methods 0.000 claims abstract description 18
- 238000010000 carbonizing Methods 0.000 claims abstract description 15
- 239000012452 mother liquor Substances 0.000 claims abstract description 15
- 239000007921 spray Substances 0.000 claims description 19
- 239000007789 gas Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 13
- 238000012856 packing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 31
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 abstract description 20
- 229910052748 manganese Inorganic materials 0.000 abstract description 20
- 239000011572 manganese Substances 0.000 abstract description 20
- ISPYRSDWRDQNSW-UHFFFAOYSA-L manganese(II) sulfate monohydrate Chemical compound O.[Mn+2].[O-]S([O-])(=O)=O ISPYRSDWRDQNSW-UHFFFAOYSA-L 0.000 abstract description 19
- 235000006748 manganese carbonate Nutrition 0.000 abstract description 17
- 239000011656 manganese carbonate Substances 0.000 abstract description 17
- 229940093474 manganese carbonate Drugs 0.000 abstract description 17
- 229910000016 manganese(II) carbonate Inorganic materials 0.000 abstract description 17
- XMWCXZJXESXBBY-UHFFFAOYSA-L manganese(ii) carbonate Chemical compound [Mn+2].[O-]C([O-])=O XMWCXZJXESXBBY-UHFFFAOYSA-L 0.000 abstract description 17
- 229940099596 manganese sulfate Drugs 0.000 abstract description 7
- 235000007079 manganese sulphate Nutrition 0.000 abstract description 7
- 239000011702 manganese sulphate Substances 0.000 abstract description 7
- 238000003763 carbonization Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 abstract 1
- 238000002425 crystallisation Methods 0.000 abstract 1
- 230000008025 crystallization Effects 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- 239000000706 filtrate Substances 0.000 description 15
- 238000001556 precipitation Methods 0.000 description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 10
- 229940075933 dithionate Drugs 0.000 description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 8
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 8
- 239000004411 aluminium Substances 0.000 description 8
- 229910052782 aluminium Inorganic materials 0.000 description 8
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 8
- 239000011575 calcium Substances 0.000 description 8
- 229910052791 calcium Inorganic materials 0.000 description 8
- 238000005119 centrifugation Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 8
- 229910001385 heavy metal Inorganic materials 0.000 description 8
- 150000002500 ions Chemical class 0.000 description 8
- 229910052742 iron Inorganic materials 0.000 description 8
- 239000011777 magnesium Substances 0.000 description 8
- 229910052749 magnesium Inorganic materials 0.000 description 8
- 239000007787 solid Substances 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 5
- 235000011941 Tilia x europaea Nutrition 0.000 description 5
- 239000003517 fume Substances 0.000 description 5
- 239000004571 lime Substances 0.000 description 5
- 239000013049 sediment Substances 0.000 description 5
- 235000017550 sodium carbonate Nutrition 0.000 description 5
- 229910000029 sodium carbonate Inorganic materials 0.000 description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000001238 wet grinding Methods 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- FWFGVMYFCODZRD-UHFFFAOYSA-N oxidanium;hydrogen sulfate Chemical compound O.OS(O)(=O)=O FWFGVMYFCODZRD-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model discloses SO in a kind of pyrolusite pulp removing flue gas2And its device of recycling, including pressurization blower, desulfurizing tower, demister, stock pump I, circulating pump, surge tank, desulfurization slurry storage tank, stock pump II, vacuum filter I, dump tank I, vavuum pump I, purification tank, screw pump, filter press, neutralization chamber, clarification sedimentation basin, stock pump III, vacuum filter II, dump tank II, vavuum pump II, cold boiler, centrifuge I, clear liquid pump, carbonizing trough, centrifuge II, mother liquor tank, ammonia pump, ammonia still, dephlegmator, drying machine I, drying machine II；Device is using the SO in manganese ore slurry removing flue gas2, reaction generation manganese sulfate, by the techniques such as purification, evaporative crystallization and mother liquor carbonization, the manganese sulfate monohydrate and manganese carbonate of acquisition high added value, to the SO in flue gas2Administered, prevented the secondary pollution of flue gas, while high value added product is generated, while solving SO2Governing problem.
Description
Technical field
The utility model is related to SO in a kind of pyrolusite removing flue gas2And its device of recycling, reach with raw ore
The purpose of pollution treatment, while obtaining high value-added product, belongs to environmental protection technical field.
Background technology
Fume desulphurization method is mutually classified by the thing of desulfurizing agent, is broadly divided into dry desulfurization and the class of wet desulphurization two.At present
Domestic and international flue gas desulfurization skill technological process kind more than 200, technique and its corollary equipment with industrial application value only ten
Remaining kind.Wet desulphurization is simple to operate, low cost, the most commonly used.In Wet Flue Gas Desulfurization Technique, although lime-limestone-based process is current
Technology is the most ripe, and the technique desulfuration efficiency (desulfurization degree more than 90%) high, absorbent are inexpensive and source is wide, but its system is multiple
Miscellaneous, investment and energy consumption are big, and production waste residue application value less, easily causes secondary pollution；Ammonia absorption method (sour method) accessory substance
Though can be used as fertilizer, with ammonia loss by volatilization during desulfurization, and limited by ammonia source again；Other sodium methods or Dual alkali cost are same
Height, also less, enterprise is economically under great stress for by-product utilization value, perfect with environmental regulation, finds new
Sulfur removal technology and equipment are imperative.
China's promoter manganese enriches, distributed more widely, cheap, using the sulfur dioxide in manganese ore slurry removing flue gas, both disappears
Except environmental pollution, and resourcebility utilizes SO2, while improving pyrolusite added value, enterprise can obtain additional economic benefit, and simultaneously
There is no set of appliance arrangement preferably to carry out the flue gas desulfurization technique of pyrolusite, while proposing SO2It is reacted with pyrolusite
The method and approach and apparatus of the purifies and separates of product, the further manganese sulfate of production high added value and manganese carbonate.
The characteristics of present apparatus is：(1) in sweetening process, the slurries after desulfurization are filtered by stock pump to vacuum filter,
PH is adjusted by lime is heated, added in purification tank, be filtered to remove manganous dithionate again, then it is heavy by neutralization chamber ammonification water and clarification
Form sediment, filtering removes other metal impurities, obtains manganese sulfate clear liquid, clear liquid carries out vacuum evaporating crystalization, is separated with centrifuge while hot,
Manganese sulfate monohydrate is obtained with microwave drying；Evaporation Mother liquor, by adding soda ash, produces manganese carbonate precipitation in carbonizing trough, uses centrifuge
Separate, filter cake obtains manganese carbonate through microwave drying.
The content of the invention
The purpose of this utility model is to provide SO in the manganese ore slurry removing flue gas2With the device of recycling, bag
Include pressurization blower 1, desulfurizing tower 2, demister 3, stock pump I4, circulating pump 5, surge tank 6, desulfurization slurry storage tank 7, stock pump II8, vacuum
Filter I9, dump tank I10, vavuum pump I11, purification tank 12, screw pump 13, filter press 14, neutralization chamber 15, clarification sedimentation basin
16th, stock pump III17, vacuum filter II18, dump tank II19, vavuum pump II20, cold boiler 21, centrifuge I22, clear liquid
Pump 23, carbonizing trough 24, centrifuge II25, mother liquor tank 26, ammonia pump 27, ammonia still 28, dephlegmator 29, drying machine I30, drying machine
II31；
Pressurization blower 1 is connected with the bottom of desulfurizing tower 2, and the bottom of desulfurizing tower 2 is provided with material box, and top is provided with spray equipment,
Material box is connected with circulating pump 5, and circulating pump 5 is connected with spray equipment, and the top of desulfurizing tower 2 is provided with exhanst gas outlet, exhanst gas outlet with
Demister 3 is connected, and the bottom material box of desulfurizing tower 2 is also connected with stock pump I 4, the connection surge tank 6 of stock pump I 4, the bottom material box of desulfurizing tower 2
Also it is connected with desulfurization slurry storage tank 7, desulfurization slurry storage tank 7 is connected by stock pump II 8 with vacuum filter I 9, and vacuum filter I 9 is connected
Dump tank I 10, the top of dump tank I 10 is connected with vavuum pump I 11, the bottom of dump tank I 10 connection purification tank 12, the bottom of purification tank 12
Filter press 14 is connected by screw pump 13, the connection neutralization chamber 15 of filter press 14, the bottom of neutralization chamber 15 connection clarification sedimentation basin 16 is clear
Clear sedimentation basin 16 connects vacuum filter II 18, the connection dump tank II 19 of vacuum filter II 18, dump tank by stock pump III 17
II 19 tops are connected with vavuum pump II 20, and the bottom of dump tank II 19 is sequentially connected cold boiler 21, centrifuge I 22, centrifugation
Machine I 22 is connected with drying machine II 31 and clear liquid pump 23 respectively, and clear liquid pump 23 is sequentially connected carbonizing trough 24, centrifuge II 25, is centrifuged
Machine II 25 connects drying machine I 30 and mother liquor tank 26 respectively, and mother liquor tank 26 is sequentially connected ammonia pump 27, ammonia still 28, dephlegmator
29, dephlegmator 29 is connected with neutralization chamber 15.
Honeycomb inclined plate packing is provided with the clarification sedimentation basin 16.
Agitating paddle is equipped with inside the surge tank 6, desulfurization slurry storage tank 7, purification tank 12, neutralization chamber 15, carbonizing trough 24.
Neutralization chamber 15 is back to through the raising ammonia density of dephlegmator 29 up to 10% or so steam containing ammonia to recycle.
Using SO in described device kind manganese ore slurry removing flue gas2And its method for recycling, comprise the following steps that：
(1) pyrolusite is utilized into ball mill wet-milling, crosses 200 mesh sieves, added water and be made pyrolusite pulp, pyrolusite pulp solid content is
18~22%, regulation pyrolusite pulp pH value is 3.5~4.5；
(2) temperature flue gas higher initially enters afterheat heat exchanger generation low-pressure steam and is used for evaporization process, after cooling
Flue gas from desulfurizing tower bottom enter, pyrolusite pulp obtained in step (1) is evacuated to desulfurizing tower 2 and is sprayed, flue gas with spray
The reverse haptoreaction of manganese ore slurry, after flue gas desulfurization from exhanst gas outlet out, flue gas enters subsequent processing or direct after demister 3
Emptying, slurries carry out slurries replacing supplement in spray through circulated sprinkling, and technique is carried out continuously, main in the slurries after circulation
It is manganese sulfate, next to that ferric sulfate, also containing a small amount of calcium, magnesium, iron, aluminium and a small amount of heavy metal ion, also contains desulfurization
During the manganous dithionate that generates, slurries carry out vacuum filter；
(3) it is 4.5~5 that step (2) is filtrated to get filtrate adds lime regulation pH value, then with being steam heated to 70~80
DEG C, manganous dithionate is decomposed, staticly settle, sediment is filtered, obtain purifying filter liquor；
(4) purifying filter liquor of step (3) is poured into neutralization chamber 15, add ammoniacal liquor, adjustment pH value be 5~5.5, make calcium,
Magnesium, iron, aluminium and a small amount of heavy metal ion generation hydroxide precipitation, neutralizer are put into clarification sedimentation basin 16, precipitation
Clarification, and further filtered with vacuum filter II18, obtain clear liquid；
(5) clear liquid of step (4) being carried out into vacuum evaporating crystalization with cold boiler 21, vacuum is 0.07~
0.08MPa, temperature is 70~80 DEG C, and manganese sulfate monohydrate mass concentration is concentrated into 38~40% (wt%), and centrifugation point is carried out while hot
From obtaining manganese sulfate monohydrate after filter residue and drying；
(6) step (5) separating obtained filtrate after cooling, adds soda ash, produces manganese carbonate precipitation, carries out separation of solid and liquid,
Filter residue and drying obtains manganese carbonate, and separating filtrate uses direct steam heating, the mixture warp point contracting of ammonia and steam in ammonia still 28
Device 29, controls dephlegmator outlet temperature, and ammonia returns to neutralization chamber 15 and recycles.
Step (6) is described to control the outlet temperature of dephlegmator 29 for 80~95 DEG C.
Advantage of the present utility model：
1. using pyrolusite as desulfurizing agent, to the SO in flue gas2Administered, prevented the secondary pollution of flue gas, realize with
The purpose of useless pollution treatment, realizes the purpose of environmental protection.
2. in sweetening process, while the manganese dioxide in recycling pyrolusite generates an added value water sulphur higher
Sour manganese and manganese carbonate, remove SO2While take full advantage of pyrolusite resource, make the best use of everything, realize the mesh of recycling
's.
3., using manganese ore as desulfurizing agent, operating cost is low；Carry out recycling simultaneously, produce high attached by desulfurization product
Value added manganese sulfate monohydrate and manganese carbonate, improving enterprise has obvious economic benefit, recycles 1 ton of SO2, can make a profit 3000~
3500 yuan, environmental pollution improvement does not spend, and has good economic benefit.
Brief description of the drawings
Fig. 1 is the structural representation of device described in the utility model；
In figure, 1- pressurization blowers；2- desulfurizing towers；3- demisters；4- stock pumps I；5- circulating pumps；6- surge tanks；7- desulfurization
Slurry storage tank；8- stock pumps II；9- vacuum filters I；10- dump tanks I；11- vavuum pumps I；12- purification tanks；13- screw pumps；14- is pressed
Filter；15- neutralization chambers；16- clarifies sedimentation basin；17- stock pumps III；18- vacuum filters II；19- dump tanks II；20- vavuum pumps
II；21- cold boilers；22- centrifuges I；23- clear liquid pumps；24- carbonizing troughs；25- centrifuges II；26- mother liquor tanks；27- ammonias
Pump；28- ammonia stills；29- dephlegmators；30- drying machines I；31- drying machines II.
Specific embodiment
Below in conjunction with the accompanying drawings and specific embodiment, the utility model is described in further detail.
Embodiment 1
As shown in figure, SO in a kind of manganese ore slurry removing flue gas2And its device of recycling, including pressurization blower
1st, desulfurizing tower 2, demister 3, stock pump I4, circulating pump 5, surge tank 6, desulfurization slurry storage tank 7, stock pump II8, vacuum filter I9, connect
Groove I10, vavuum pump I11, purification tank 12, screw pump 13, filter press 14, neutralization chamber 15, clarification sedimentation basin 16, stock pump III17,
Vacuum filter II18, dump tank II19, vavuum pump II20, cold boiler 21, centrifuge I22, clear liquid pump 23, carbonizing trough
24th, centrifuge II25, mother liquor tank 26, ammonia pump 27, ammonia still 28, dephlegmator 29, drying machine I30, drying machine II31；Pressurization drum
Blower fan 1 is connected with the bottom of desulfurizing tower 2, and the bottom of desulfurizing tower 2 is provided with material box, and top is provided with spray equipment, material box and circulating pump 5
Connection, circulating pump 5 is connected with spray equipment, and spray equipment is provided with three rows in different height, often arranges 5 shower nozzles, the top of desulfurizing tower 2
Exhanst gas outlet is provided with, exhanst gas outlet is connected with demister 3, the bottom material box of desulfurizing tower 2 is also connected with stock pump I 4, the connection of stock pump I 4 is adjusted
Stock tank 6, the bottom material box of desulfurizing tower 2 is also connected with desulfurization slurry storage tank 7, and desulfurization slurry storage tank 7 passes through stock pump II 8 and vacuum filter
I 9 connections, the connection dump tank I 10 of vacuum filter I 9, the top of dump tank I 10 is connected with vavuum pump 11, bottom connection purification tank
12, the bottom of purification tank 12 connects filter press 14, the connection neutralization chamber 15 of filter press 14, the connection of the bottom of neutralization chamber 15 by screw pump 13
Clarification sedimentation basin 16, is provided with honeycomb inclined plate packing in clarification sedimentation basin 16, clarification sedimentation basin 16 connects vacuum by stock pump III 17
Filter II 18, the connection dump tank II 19 of vacuum filter II 18, the top of dump tank II 19 is connected with vavuum pump II20, dump tank
II 19 bottoms are sequentially connected cold boiler 21, centrifuge I22, and centrifuge I22 is connected with drying machine II31 and clear liquid pump 23 respectively,
Clear liquid pump 23 is sequentially connected carbonizing trough 24, centrifuge II25, and centrifuge II 25 connects drying machine II 30 and mother liquor tank 26 respectively,
Mother liquor tank 26 is sequentially connected ammonia pump 27, ammonia still 28, dephlegmator 29, and dephlegmator 29 is connected with neutralization chamber 15, surge tank 6, de-
Agitating paddle is equipped with inside sulphur slurry storage tank 7, purification tank 12, neutralization chamber 15, carbonizing trough 24.
Using said apparatus carry out manganese ore slurry removing flue gas in SO2And its method for recycling, comprise the following steps that：
(1) pyrolusite is utilized into ball mill wet-milling, crosses 200 mesh sieves, added water in surge tank 6 and be made pyrolusite pulp, soft manganese
Ore pulp solid content is 20% (wt%), and regulation pyrolusite pulp pH value is 3.5；
(2) flue gas is that anode calcines flue gas, exhaust gas volumn 60000Nm3/ h, SO in flue gas2Content is 3000mg/Nm3, averagely
220 DEG C of temperature, it is desirable to discharge flue gas SO2Less than 100mg/Nm3, it is low that temperature flue gas higher initially enters afterheat heat exchanger generation
Pressure steam is used for evaporization process, and the pressurized air blower 1 of flue gas enters from the bottom of desulfurizing tower 2 after cooling, and step (1) is obtained
Pyrolusite pulp is evacuated to desulfurizing tower 2 and is sprayed with spray equipment with circulating pump 5, and spray equipment is provided with three rows in different height, often
5 shower nozzles of row, flue gas and the reverse haptoreaction of manganese ore slurry for spraying, after flue gas desulfurization from exhanst gas outlet out, through demister 5
Afterwards, flue gas SO2Content is 90mg/Nm3, discharge up to standard, directly empty, serum recycle spray, while spray while carry out slurries discharge and
Supplement, technique is carried out continuously, and manganese sulfate is mainly in the slurries after circulation, next to that ferric sulfate, also containing a small amount of calcium, magnesium,
Iron, aluminium and a small amount of heavy metal ion, also containing the manganous dithionate generated in sweetening process, slurry storage is starched in desulfurization and store
In groove 7, being evacuated to vacuum filter I9 through stock pump II8 carries out vacuum filter, is filtrated to get filtrate into dump tank I10；
(3) filtrate that step (2) is filtrated to get enters in purification tank 12 from dump tank I10, and purification tank 12 is provided with agitating paddle,
Add lime to adjust slurry pH value to 5 while stirring, then 80 DEG C are steam heated to what fume afterheat was produced, make manganous dithionate
Decompose, slurries are evacuated to filter press 14, sediment is filtered through screw pump 13, obtain purifying filter liquor into neutralization chamber 15；
(4) by step (3) neutralization chamber 15 purifying filter liquor add ammoniacal liquor, adjustment pH value be 5, make calcium, magnesium, iron, aluminium with
And a small amount of heavy metal ion generation hydroxide precipitation, neutralizer is put into clarification sedimentation basin 16, filled out using honeycomb swash plate
Material carries out precipitation clarification, and liquid is evacuated into vacuum filter II18 with stock pump III17 further filters, and obtains clear liquid and enters and connects
Groove II19；
(5) clear liquid in step (4) dump tank II19 is carried out into vacuum evaporating crystalization through cold boiler 21, is evaporated in vacuo
The vacuum of device 21 is 0.08MPa, and temperature is 80 DEG C, and manganese sulfate monohydrate mass percentage concentration is concentrated into 38% (wt%), while hot
It is centrifuged through centrifuge I22, filter residue obtains manganese sulfate monohydrate after being dried through drying machine II31, and sulfuric acid monohydrate is produced every year
2000 tons or so of manganese；
(6) step (5) centrifugation gained filtrate after cooling, through clear liquid pump 23 into adding soda ash after carbonizing trough 24,
Manganese carbonate precipitation is produced, centrifuge II25 centrifugations carry out separation of solid and liquid, and filter residue is dried to obtain manganese carbonate, filtrate through drying machine I30
Into mother liquor tank 26, it is evacuated in ammonia still 28 through ammonia pump 27, the steam produced with direct fume afterheat is heated, ammonia and steam
Mixture is through dephlegmator 29,80 DEG C of 29 exit gas temperature of control dephlegmator, during ammonia density is back to up to 10% (wt%) left and right
Recycled with groove 15, annual 2100 tons or so of manganese carbonate of production.
Embodiment 2
SO in manganese ore slurry removing flue gas described in the present embodiment2And its method for recycling, using device and embodiment 1
Except setting two row's spray equipments, often row is set outside 7 shower nozzles, and other all sames are comprised the following steps that：
(1) pyrolusite is utilized into ball mill wet-milling, crosses 200 mesh sieves, added water in surge tank 6 and be made pyrolusite pulp, soft manganese
Ore pulp solid content is 22% (wt%), and regulation pyrolusite pulp pH value is 4；
(2) flue gas is boiler of power plant flue gas, exhaust gas volumn 100000Nm3/ h, SO in flue gas2Content is 2000mg/Nm3, averagely
120 DEG C of temperature, it is desirable to discharge flue gas SO2Less than 400mg/Nm3, it is low that temperature flue gas higher initially enters afterheat heat exchanger generation
Pressure steam is used for evaporization process, and the pressurized air blower 1 of flue gas enters from the bottom of desulfurizing tower 2 after cooling, and step (1) is obtained
Pyrolusite pulp is evacuated to desulfurizing tower 2 and is sprayed with spray equipment with circulating pump 5, and flue gas is reverse with the manganese ore slurry of spray to contact anti-
Should, after flue gas desulfurization from exhanst gas outlet out, the SO after demister 5 in flue gas2Absorbed, removed SO2Flue gas SO afterwards2Contain
It is 300mg/Nm to measure3, flue gas discharge up to standard directly empties, and slurries carry out slurries discharge and benefit through circulated sprinkling in spray
Fill, technique is carried out continuously, manganese sulfate be mainly in the slurries after circulation, next to that ferric sulfate, also containing a small amount of calcium, magnesium, iron,
Aluminium and a small amount of heavy metal ion, also containing the manganous dithionate generated in sweetening process, slurry storage starches storage tank 7 in desulfurization
Interior, being evacuated to vacuum filter I9 through stock pump II8 carries out vacuum filter, is filtrated to get filtrate into dump tank I10；
(3) filtrate that step (2) is filtrated to get enters in purification tank 12 from dump tank I10, and purification tank 12 is provided with agitating paddle,
Add lime to adjust slurry pH value to 4.5, then with being steam heated to 70 DEG C while stirring, decompose manganous dithionate, slurries warp
Screw pump 13 is evacuated to filter press 14, and sediment is filtered, and obtains purifying filter liquor into neutralization chamber 15；
(4) purifying filter liquor in step (3) neutralization chamber 15 is added into ammoniacal liquor, adjustment pH value is 5.5, makes calcium, magnesium, iron, aluminium
And a small amount of heavy metal ion generation hydroxide precipitation, neutralizer is put into clarification sedimentation basin 16, using honeycomb swash plate
Filler carries out the precipitation clarification of long period, and liquid is evacuated into vacuum filter II18 with stock pump III17 further filters, and obtains
Obtain clear liquid and enter dump tank II19；
(5) clear liquid in step (4) dump tank II19 is carried out into vacuum evaporating crystalization through cold boiler 21, is evaporated in vacuo
The vacuum of device 21 is 0.07MPa, and temperature is 70 DEG C, and manganese sulfate monohydrate concentration is concentrated into 39% (wt%), while hot through centrifuge
I22 is centrifuged, and filter residue obtains manganese sulfate monohydrate after being dried through drying machine II31, annual 180 tons of manganese sulfate monohydrate of production
Left and right；
(6) step (5) centrifugation gained filtrate after cooling, through clear liquid pump 23 into adding soda ash after carbonizing trough 24,
Manganese carbonate precipitation is produced, centrifuge II25 centrifugations carry out separation of solid and liquid, and filter residue is dried to obtain manganese carbonate, filtrate through drying machine I30
Into mother liquor tank 26, it is evacuated in ammonia still 28 through ammonia pump 27, the steam produced with direct fume afterheat is heated, ammonia and steam
Mixture is through dephlegmator 29,90 DEG C of 29 exit gas temperature of control dephlegmator, during ammonia density is back to up to 10% (wt%) left and right
Recycled with groove, annual 1900 tons or so of manganese carbonate of production.
Embodiment 3
SO in manganese ore slurry removing flue gas described in the present embodiment2And its method for recycling, using device and embodiment 1
Identical device, comprises the following steps that：
(1) pyrolusite is utilized into ball mill wet-milling, crosses 200 mesh sieves, added water in surge tank 6 and be made pyrolusite pulp, soft manganese
Ore pulp solid content is 18% (wt%), and regulation pyrolusite pulp pH value is 4.5；
(2) flue gas is that sulfuric acid prepares factory's flue gas, sulfuric acid tail gas treating capacity 200000Nm3/ h, double-absorption sulfuric acid apparatus
SO in tail gas2Content 650mg/Nm3, offgas outlet requirement SO2Content 100mg/Nm3Hereinafter, desulfuration efficiency more than 85%, temperature
Flue gas higher initially enters afterheat heat exchanger and produces low-pressure steam to be used for evaporization process, the pressurized air blower of flue gas after cooling
1 enters from the bottom of desulfurizing tower 2, pyrolusite pulp obtained in step (1) is evacuated into desulfurizing tower and is sprayed, the manganese ore of flue gas and spray
Reverse haptoreaction is starched, after flue gas desulfurization from exhanst gas outlet out, the SO after demister 5 in flue gas2Absorbed, removed SO2Afterwards
Flue gas SO2Content is 300mg/Nm3, flue gas is up to standard to be discharged into next treatment process, slurries through circulated sprinkling, in spray
Discharge and the supplement of slurries are carried out, technique is carried out continuously, manganese sulfate is mainly in the slurries after circulation, next to that ferric sulfate, also
Contain a small amount of calcium, magnesium, iron, aluminium and a small amount of heavy metal ion, also containing the manganous dithionate generated in sweetening process, slurry
Liquid is stored in desulfurization slurry storage tank 7, and being evacuated to vacuum filter I9 through stock pump II8 carries out vacuum filter, is filtrated to get filtrate entrance
Dump tank I10；
(3) filtrate that step (2) is filtrated to get enters in purification tank 12 from dump tank I10, and purification tank 12 is provided with agitating paddle,
Add lime to adjust slurry pH value to 4.5, then with being steam heated to 75 DEG C while stirring, decompose manganous dithionate, slurries warp
Screw pump 13 is evacuated to filter press 14, and sediment is filtered, and obtains purifying filter liquor into neutralization chamber 15；
(4) by step (3) neutralization chamber 15 purifying filter liquor add ammoniacal liquor, adjustment pH value be 5, make calcium, magnesium, iron, aluminium with
And a small amount of heavy metal ion generation hydroxide precipitation, neutralizer is put into clarification sedimentation basin 16, filled out using honeycomb swash plate
Material carries out precipitation clarification, and liquid is evacuated into vacuum filter II18 with stock pump III17 further filters, and obtains clear liquid and enters and connects
Groove II19；
(5) clear liquid in step (4) dump tank II19 is carried out into vacuum evaporating crystalization through cold boiler 21, is evaporated in vacuo
The vacuum of device 21 is 0.08Mpa, and temperature is 75 DEG C, and manganese sulfate monohydrate mass percentage concentration is concentrated into 40% (wt%), while hot
It is centrifuged through centrifuge I22, filter residue obtains manganese sulfate monohydrate after being dried through drying machine II31, and sulfuric acid monohydrate is produced every year
1800 tons or so of manganese；
(6) step (5) centrifugation gained filtrate after cooling, through clear liquid pump 23 into adding soda ash after carbonizing trough 24,
Manganese carbonate precipitation is produced, centrifuge II25 centrifugations carry out separation of solid and liquid, and filter residue is dried to obtain manganese carbonate, filtrate through drying machine I30
Into mother liquor tank 26, it is evacuated in ammonia still 28 through ammonia pump 27, the steam produced with direct fume afterheat is heated, ammonia and steam
Mixture controls 95 DEG C of 29 exit gas temperature of dephlegmator through dephlegmator 29, and ammonia density is back to neutralization chamber and follows up to 10% or so
Ring is used, annual 1500 tons or so of manganese carbonate of production.
Above-described is only implementation method of the present utility model, it is noted that for one of ordinary skill in the art
For, on the premise of the utility model creation design is not departed from, various modifications and improvements can be made, these belong to this
The protection domain of utility model.
Claims (3)
1. a kind of pyrolusite pulp removes SO in flue gas2And its device of recycling, it is characterised in that including pressurization blower,
Desulfurizing tower, demister, stock pump I, circulating pump, surge tank, desulfurization slurry storage tank, stock pump II, vacuum filter I, dump tank I, vacuum
Pump I, purification tank, screw pump, filter press, neutralization chamber, clarification sedimentation basin, stock pump III, vacuum filter II, dump tank II, vacuum
It is pump II, cold boiler, centrifuge I, clear liquid pump, carbonizing trough, centrifuge II, mother liquor tank, ammonia pump, ammonia still, dephlegmator, dry
Dry machine I, drying machine II；
Pressurization blower is connected with desulfurizing tower bottom, and desulfurization tower bottom is provided with material box, and top is provided with spray equipment, material box with
Circulating pump is connected, and circulating pump is connected with spray equipment, and desulfurizing tower top exhanst gas outlet is connected with demister, desulfurization tower bottom charge
Case is also connected with stock pump I, and the connection surge tank of stock pump I, desulfurization tower bottom material box is also connected with desulfurization slurry storage tank, and desulfurization slurry storage tank leads to
Cross stock pump II to be connected with vacuum filter I, the connection dump tank I of vacuum filter I, dump tank I is connected with vavuum pump I, dump tank I
Bottom connects purification tank, and purification trench bottom connects filter press by screw pump, and filter press connection neutralization chamber neutralizes trench bottom connection
Clarification sedimentation basin, clarification sedimentation basin connects vacuum filter II by stock pump III, and the connection dump tank II of vacuum filter II receives
Groove II is connected with vavuum pump II, and the bottom of dump tank II is sequentially connected cold boiler, centrifuge I, and centrifuge I is connected with drying respectively
Machine II and clear liquid pump, clear liquid pump are sequentially connected carbonizing trough, centrifuge II, and centrifuge II connects drying machine I and mother liquor tank respectively, female
Liquid bath is sequentially connected ammonia pump, ammonia still, dephlegmator, and dephlegmator is connected with neutralization chamber.
2. pyrolusite pulp removes SO in flue gas according to claim 12And its device of recycling, it is characterised in that institute
State in clarification sedimentation basin and be provided with honeycomb inclined plate packing.
3. pyrolusite pulp removes SO in flue gas according to claim 12And its device of recycling, it is characterised in that institute
State and be equipped with agitating paddle inside surge tank, desulfurization slurry storage tank, purification tank, neutralization chamber, carbonizing trough.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621151643.7U CN206304563U (en) | 2016-10-31 | 2016-10-31 | SO in a kind of pyrolusite pulp removing flue gas2And its device of recycling |
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| CN201621151643.7U CN206304563U (en) | 2016-10-31 | 2016-10-31 | SO in a kind of pyrolusite pulp removing flue gas2And its device of recycling |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106377993A (en) * | 2016-10-31 | 2017-02-08 | 昆明理工大学 | Method and device for removing SO2 in smoke gas by pyrolusite slurry and resource utilization |
| CN109847550A (en) * | 2019-01-23 | 2019-06-07 | 昆明理工大学 | A kind of phase interface regulation improves the method and application of pyrolusite dreg slurry desulfuration efficiency |
-
2016
- 2016-10-31 CN CN201621151643.7U patent/CN206304563U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106377993A (en) * | 2016-10-31 | 2017-02-08 | 昆明理工大学 | Method and device for removing SO2 in smoke gas by pyrolusite slurry and resource utilization |
| CN109847550A (en) * | 2019-01-23 | 2019-06-07 | 昆明理工大学 | A kind of phase interface regulation improves the method and application of pyrolusite dreg slurry desulfuration efficiency |
| CN109847550B (en) * | 2019-01-23 | 2021-09-24 | 昆明理工大学 | Method for improving pyrolusite slag slurry desulfurization efficiency through phase interface regulation and control and application |
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