CN201942526U - System for directly producing sodium sulfite from sulfur-containing acidic gas - Google Patents
System for directly producing sodium sulfite from sulfur-containing acidic gas Download PDFInfo
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- CN201942526U CN201942526U CN2011200036433U CN201120003643U CN201942526U CN 201942526 U CN201942526 U CN 201942526U CN 2011200036433 U CN2011200036433 U CN 2011200036433U CN 201120003643 U CN201120003643 U CN 201120003643U CN 201942526 U CN201942526 U CN 201942526U
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- sulfur
- absorption tower
- tank
- sodium sulfite
- gas
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- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 title claims abstract description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 23
- 239000011593 sulfur Substances 0.000 title claims abstract description 23
- 235000010265 sodium sulphite Nutrition 0.000 title abstract description 10
- 230000002378 acidificating effect Effects 0.000 title abstract 4
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000005406 washing Methods 0.000 claims abstract description 20
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 21
- 239000002253 acid Substances 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 11
- 239000005864 Sulphur Substances 0.000 claims description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 8
- 238000006477 desulfuration reaction Methods 0.000 abstract description 8
- 230000023556 desulfurization Effects 0.000 abstract description 6
- 238000002425 crystallisation Methods 0.000 abstract description 4
- 230000008025 crystallization Effects 0.000 abstract description 4
- 238000006386 neutralization reaction Methods 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 45
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 36
- 239000007789 gas Substances 0.000 description 33
- 235000017550 sodium carbonate Nutrition 0.000 description 18
- 229910000029 sodium carbonate Inorganic materials 0.000 description 18
- 235000011121 sodium hydroxide Nutrition 0.000 description 16
- 238000000034 method Methods 0.000 description 15
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 11
- 239000012452 mother liquor Substances 0.000 description 9
- 239000000047 product Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 4
- 235000011089 carbon dioxide Nutrition 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 4
- JXAZAUKOWVKTLO-UHFFFAOYSA-L sodium pyrosulfate Chemical compound [Na+].[Na+].[O-]S(=O)(=O)OS([O-])(=O)=O JXAZAUKOWVKTLO-UHFFFAOYSA-L 0.000 description 4
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 235000012204 lemonade/lime carbonate Nutrition 0.000 description 3
- 229910052750 molybdenum Inorganic materials 0.000 description 3
- 239000011733 molybdenum Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 241001253206 Andrias Species 0.000 description 1
- 241000370738 Chlorion Species 0.000 description 1
- 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
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 206010039509 Scab Diseases 0.000 description 1
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production 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
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000003765 sweetening agent Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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Abstract
The utility model provides a system for directly producing sodium sulfite from a sulfur-containing acidic gas. The system can not only effectively handle the sulfur-containing acidic gas but also produce a new product of sodium sulfite. The sulfur-containing acidic gas is fed to an incinerator; the incinerator is connected in series with a high-temperature dryer, a desulfurization tank, a cooler and a water washing tank; the water washing tank is connected with an absorption tower; the absorption tower is connected with a neutralization kettle; the neutralization kettle is connected with a filter; the filter is connected with a crystallization device; and the crystallization device is connected with a separator. The system can directly produce sodium sulfite from the recovered sulfur instead of producing sulfuric acid from the recovered sulfur or producing sodium sulfite from sulfur in the prior art.
Description
Affiliated technical field
The utility model relates to a kind ofly effectively administers and obtains the system of product innovation to the sulfur-bearing sour gas, specifically utilizes the process system of sulfur-bearing sour gas direct production S-WAT.
Background technology
Entered since 21st century, maximum in the world population is just being carried with the ecotope of most fragile in history in China, is carrying the most unprecedented in history resource consumption and economic activity, is faced with the most outstanding in history ecotope challenge.Oneself becomes the maximum restraining factors of China's Modernization development contradiction between population and resource, Economic development and the ecotope.Keep Sustainable development, just must reduce pollution and enforcement recycling economy environment.And sulfurous gas, it is one of main atmospheric polluting material of face of mankind nowadays, its existence has all caused harm to a certain degree to aspects such as natural ecological environment, human health, industrial and agricultural production, buildings and materials, once took place more than 10 times and sulfurous gas in modern age on the human history, polluted relevant major disaster.
Gas behind at present a lot of task factories cleaning section includes hydrogen sulfide and organosulfur, need enter conversion procedure and carry out desulfurization, similarly is that low-temperature rectisol is exactly to carry out the chemical reaction desulfurization with salt of wormwood then with the methyl alcohol absorbing hydrogen sulphide earlier under the low pressure.This conversion procedure finally mostly converts hydrogen sulfide to sulfuric acid or sulphur, similarly is to use super Crouse to come recovery sulphur or WSA wet method system sulfuric acid.And generally make S-WAT is directly to utilize the heating of bright sulfur sulphur to generate sulfurous gas, is that raw material production is made S-WAT then with sulfurous gas.
Similarly be in the molybdenum smelting industry; when utilizing the rotary kiln baking concentrated molybdenum ore, can produce a large amount of tail gas need the discharging, contain in this tail gas a large amount of dust and and dense sulfurous gas; in order to protect environment not contaminated, need carry out dust-removal and desulfurizing to tail gas and handle.The treatment process of its tail gas is after filtering out dust by sack cleaner, and the discharging of waste liquid with tail gas and generation after the gas that will contain sulfurous gas is sent into the absorption cleaning tower and absorbed by depletion falls.The weak point one of this kind treatment process is that the sulfurous gas in the tail gas can not obtain recycling, and can not create economic benefit again for enterprise.
In the process of producing liquefied gas and gasoline, all adopt the sodium hydroxide solution washing, to remove sour gas and impurity such as hydrogen sulfide, small molecules mercaptan and phenol.When sodium hydroxide major part in the alkali lye was converted into sodium sulphite, sodium mercaptides and phenol sodium, this alkali lye just became waste lye.Its weak point is that processing condition harshness, investment are big, working cost is high, and with the processing mode of crossing in the molybdenum smelting industry, effective constituent can not be recovered utilization.
And China's fire coal accounts for more than 70% of the disposable energy, owing to contain sulphur in the coal, so the burning back produces a large amount of sulfurous gas, thereby causes serious topsoil.In the production process of thermal power generation, coal firing boiler produces a large amount of low concentration sulfur dioxide flue gases.And a spot of sulphur trioxide, oxynitride, muriate and a large amount of dust etc. are to the deleterious material of desulfurization, sulfurous gas and nitrogen oxides pollution air, the accumulation of chlorion can be corroded sweetener, the accumulation of dust can make equipment scab, stop up, influence desulfuration efficiency, influence the normal operation of desulfurizer when serious.Therefore, the task of flue gas desulfurization is very heavy.At present, it is the effective means that reduces that sulfur dioxide emissions and acid rain forms that flue gas is carried out that desulfurization handles, and the wet flue gas of successful operation takes off the moraine technology and has comparative advantage with the calcium method.The calcium method is an absorption agent with lime carbonate (being Wingdale), and its chemical reaction is as follows:
CaCO3+SO2+1/2H2O＝CaSO3·1/2H2O+CO2
2CaSO4+1/2H2O+3H2O＝2CaSO4·2H2O
Lime carbonate (being Wingdale) is water-soluble very low material, during as absorption agent, is that it is ground into powder, forms with water that slurries implement: because solid matter is arranged, and very high to the requirement of spraying equipment and handling equipment.The calcium sulfate that generates after product calcium sulfite behind the absorption sulfurous gas and the oxidation all is the very little material of solubleness, easy blocking pipe and equipment, and the gypsum of output is of poor quality because of it, and the product sales resistance can only be made emission treatment.Therefore, the lime carbonate price is low though the calcium method has, technology maturation, desulfuration efficiency height and the good advantage of social benefit, has technology and equipment more complicated, fund input is big, working cost is high, do not have economic benefit, can't break away from the shortcoming of pollution treatment manufacturing loss.
Summary of the invention
In order to overcome the deficiency of existing fume desulphurization method, the utility model provides a kind of process system that utilizes sulfur-bearing sour gas direct production S-WAT, this system not only can effectively effectively administer the sulfur-bearing sour gas, and can obtain the product innovation S-WAT simultaneously.
This technical scheme of testing that novel its technical problem of solution adopted is: the sulfur-bearing sour gas is connected to incinerator, be connected to high and dry device, sulphur removal jar, water cooler and water washing tank series connection, water washing tank is connected to the absorption tower, during the absorption tower is connected to and still, in and still be connected to strainer, strainer is connected to crystallizer, and crystallizer is connected to separator.Sulfurous gas can produce sulfurous gas through burning:
S+H2S+COS (organosulfur)-SO2
Main absorption tower, acid storage and in and still series connection.There are main absorption tower and secondary absorption tower in the absorption tower, has circulation tank connecting between main absorption tower and the secondary absorption tower.Sulfurous gas can generate S-WAT, sodium bisulfite and carbonic acid gas with the aqueous sodium carbonate reaction:
SO2+Na2CO3->Na2SO3+CO2
SO2+Na2CO3(aq)->NaHSO3+CO2
In and still neutralize by soda ash or caustic soda, after the neutralization sodium sulfite solution can in and carry out Shen in sedimentation or the sedimentation tank in the still and fall subsequent filtration.Wherein sodium pyrosulfate can generate sodium bisulfite and water with the sodium hydroxide reaction:
NaHSO3+NaOH->Na2SO3+H2O
Crystallizer concentrates S-WAT by thermal dehydration.Separator is a centrifugal separator, and the S-WAT crystallization obtains the S-WAT product with solution separating in whizzer.Mode is in the past made sulfuric acid or is made S-WAT by sulphur by reclaiming sulphur, and directly generates S-WAT by flowing back to receive now.
Owing to adopt technique scheme, the process system that utilizes sulfur-bearing sour gas direct production S-WAT that the utility model provides has such beneficial effect, promptly can directly administer by the acid gas generation S-WAT of sulfur-bearing and to the sulfur-bearing sour gas.
Description of drawings
Below in conjunction with drawings and Examples the utility model is further specified.
Figure is the utility model case process figure.
1. incinerators among the figure, 1-1. high pressure centrifugal ventilator, 2. sulphur removal jar, 3. water cooler, 4a, b, c. water washing tank, 5. main absorption tower, 5-1. jar at the bottom of the king-tower, 6. attached absorption tower, jar, 7. circulation tank at the bottom of the attached tower of 6-1., 7-1. recycle pump, 8. acid storage, 8-1. acid pump, 9-1. in and still, 9-2. soda ash header tank, 9-3. caustic soda header tank, 9-4. in and pump, 10. slurry tank, 11. hay tanks, 12. filtrate pump, 13. header tanks, 14. crystallizers, 15-1. condenser, 15-2. water collector, 16. whizzers, 16-1. mother liquor tank, 17-2. centrifuge mother liquor pump, 17. moisture eliminators, 17-1. dry strand cage, 18. soda ash storage tanks, 18-1. soda ash pump, 19. the caustic soda storage tank, 19-1. caustic soda pump, 20. mother liquor holding tanks, 20-1. the mother liquor pump, 21. cooling columns, 22. water jet pump tanks.
Embodiment
Said system can be realized by the following institute equipment of chatting: pending sulfur-bearing sour gas is connected to incinerator (1), and high pressure centrifugal ventilator (1-1) is connected to incinerator (1).Incinerator (1), dry strand cage (17-1) and moisture eliminator (17) series connection.Sulfur-bearing sour gas and air generate sulfurous gas in incinerator (1) reacting by heating, the extra required air of postreaction of high pressure centrifugal ventilator (1-1).The waste gas that incinerator (1) comes out meets environmental standard emptying then after twisting cage (17-1) and moisture eliminator (17) by drying.
Incinerator (1), sulphur removal jar (2) and water cooler (3) series connection.Water cooler (3) is connected respectively to the gangway of water washing tank (4a) and cooling column (21).Water washing tank (4a) is polyphone between water washing tank (4b) and the water washing tank (4c).Water washing tank (4c) connects street jar (5-1) at the bottom of the king-tower on main absorption tower (5) subsequently.The sulfurous gas that incinerator (1) comes out enters water washing tank then by sulphur removal jar (2) and water cooler (3), and (4a, b c), wash away sulfur trioxide gas in water washing tank.Water cooler (3) helps sulfurous gas and the cooling of other gas by carried the water of coming by cooling column (21), and the water of intensification is sent back to cooling column (21) cooling once again and recycled.Sulfurous gas is gone into jar (5-1) at the bottom of the king-tower by water washing tank is laggard, prepares to be absorbed into sodium pyrosulfate by the yellow soda ash washing.Jar at the bottom of the king-tower (5-1) connects acid storage (8), acid storage (8), acid pump (8-1) and in and still (9) series connection.Jar at the bottom of the king-tower (5-1) and main absorption tower (5) link, and main absorption tower (5) are connected with attached absorption tower (6), and jar (6-1) is connected at the bottom of attached absorption tower (6) and the attached tower.Circulation tank (7) and recycle pump (7-1) link, and recycle pump (7-1) connects main absorption tower (5) and attached absorption tower (6) respectively.Enter king-tower by the gas that contains sulfurous gas after the washing and partly be absorbed into sodium pyrosulfate by the yellow soda ash washing, the person of connecing flows to attached tower and absorbs once more, and gas washs once more by main absorption tower once again.Secondary tower washs the liquid that gets off and enters circulation tank, and the liquid that contains yellow soda ash in the circulation tank is used for using for king-tower and attached tower washing sulfurous gas by recycle pump.Sodium carbonate solution in the circulation tank (7) is provided by soda ash pump (18-1) by soda ash storage tank (18).Convert to contain sodium pyrosulfate the solution utmost point finally acid storage (8) by acid pump (8-1) deliver to and in and still (9).In be connected soda ash header tank (9-2), caustic soda header tank (9-3) respectively with still (9.1) and pass through in be connected slurry tank (10) with pump (9-4).Soda ash header tank (9-2) connects soda ash storage tank (18) by soda ash pump (18-1).Caustic soda header tank (9-3) connects caustic soda storage tank (19) by caustic soda pump (19-1).Slurry tank (10) and hay tank (11), filtrate pump (12), header tank (13), crystallizer (14) polyphone.In and the soda ash and the caustic soda that provide against soda ash header tank and caustic soda header tank in the still acid solution is neutralized, solution enters slurry tank sedimentation sodium sulfite solution subsequently.Solution enters header tank after filtering, to treat the generating sodium sulphite anhydrous 99.3 crystalline product in crystallizer.
Crystallizer (14) and whizzer (16), mother liquor tank (16-1), centrifuge mother liquor pump (17-2), mother liquor holding tank (20), mother liquor pump (20-1) polyphone.Crystallizer (14) in addition and condenser (15-1), water collector (15-2), water jet pump tank (22) contact.S-WAT through strainer concentrates by the steam-heated cal(l)andria dehydration in crystallizer.The liquid of sloughing in the crystallizer send the net mother liquor holding tank.The S-WAT crystallization obtains the S-WAT product with solution separating in whizzer.
Claims (4)
1. system that utilizes sulfur-bearing sour gas direct production S-WAT, it is characterized in that: the sulfur-bearing sour gas is connected to incinerator, be connected to high and dry device, sulphur removal jar, water cooler and water washing tank series connection, water washing tank is connected to the absorption tower, during the absorption tower is connected to and still, in and still be connected to strainer, strainer is connected to crystallizer, crystallizer is connected to separator.
2. the system that utilizes sulfur-bearing sour gas direct production S-WAT according to claim 1 is characterized in that: the absorption tower, acid storage and in and still series connection.
3. the system that utilizes sulfur-bearing sour gas direct production S-WAT according to claim 1 is characterized in that: there are main absorption tower and secondary absorption tower in described absorption tower, has circulation tank connecting between main absorption tower and the secondary absorption tower.
4. the system that utilizes sulfur-bearing sour gas direct production S-WAT according to claim 1 is characterized in that: described separator is a centrifugal separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011200036433U CN201942526U (en) | 2011-01-07 | 2011-01-07 | System for directly producing sodium sulfite from sulfur-containing acidic gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011200036433U CN201942526U (en) | 2011-01-07 | 2011-01-07 | System for directly producing sodium sulfite from sulfur-containing acidic gas |
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| CN201942526U true CN201942526U (en) | 2011-08-24 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102583452A (en) * | 2011-01-07 | 2012-07-18 | 北京柯兰富尔过滤技术有限公司 | Method and equipment for directly producing sodium sulfite by using sulfuric acid-containing gas |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
| CN110508116A (en) * | 2019-09-19 | 2019-11-29 | 中节能工程技术研究院有限公司 | Waste printed circuit board melting gas cleaning recovery system |
| CN112591769A (en) * | 2020-12-16 | 2021-04-02 | 湖南福千府生物科技有限公司 | Device for preparing sodium sulfite solution |
-
2011
- 2011-01-07 CN CN2011200036433U patent/CN201942526U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102583452A (en) * | 2011-01-07 | 2012-07-18 | 北京柯兰富尔过滤技术有限公司 | Method and equipment for directly producing sodium sulfite by using sulfuric acid-containing gas |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
| CN110508116A (en) * | 2019-09-19 | 2019-11-29 | 中节能工程技术研究院有限公司 | Waste printed circuit board melting gas cleaning recovery system |
| CN112591769A (en) * | 2020-12-16 | 2021-04-02 | 湖南福千府生物科技有限公司 | Device for preparing sodium sulfite solution |
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