CN203244957U - Oxidation device of ammonium sulfite - Google Patents
Oxidation device of ammonium sulfite Download PDFInfo
- Publication number
- CN203244957U CN203244957U CN 201320181977 CN201320181977U CN203244957U CN 203244957 U CN203244957 U CN 203244957U CN 201320181977 CN201320181977 CN 201320181977 CN 201320181977 U CN201320181977 U CN 201320181977U CN 203244957 U CN203244957 U CN 203244957U
- Authority
- CN
- China
- Prior art keywords
- oxidation
- slurries
- trough
- ammonium sulfite
- oxidation trough
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 185
- 230000003647 oxidation Effects 0.000 title claims abstract description 180
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 239000002002 slurry Substances 0.000 claims abstract description 68
- 238000004176 ammonification Methods 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 abstract description 33
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 32
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 abstract description 23
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 22
- 229910052921 ammonium sulfate Inorganic materials 0.000 abstract description 22
- 235000011130 ammonium sulphate Nutrition 0.000 abstract description 22
- 229910021529 ammonia Inorganic materials 0.000 abstract description 16
- 238000011084 recovery Methods 0.000 abstract description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 19
- 229910052760 oxygen Inorganic materials 0.000 description 19
- 239000001301 oxygen Substances 0.000 description 19
- 239000000463 material Substances 0.000 description 11
- 239000000243 solution Substances 0.000 description 11
- 238000004090 dissolution Methods 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 9
- 239000003546 flue gas Substances 0.000 description 9
- 230000023556 desulfurization Effects 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 230000001590 oxidative effect Effects 0.000 description 8
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 238000006213 oxygenation reaction Methods 0.000 description 5
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000003064 anti-oxidating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses an oxidation device of ammonium sulfite. The oxidation device comprises an oxidation tank provided with a slurry discharge pump at the bottom, an ammonification pipeline communicated with the top of the oxidation tank, an oxidation air pipe arranged in the oxidation tank and located at the lower part, as well as a plurality of perforated plates arranged in the oxidation tank at intervals and located in the middle. With the adoption of the oxidation device of ammonium sulfite, ammonium sulfite in an ammonium sulfate solution with high concentration can be rapidly oxidized, the recovery cost of ammonium sulfate is reduced, and ammonia escape and sulfur dioxide escape are prevented during the oxidation process.
Description
Technical field
The utility model relates to resource and environment protection field, is specifically related to the oxidation unit of the ammonium sulfite in a kind of ammonia process of desulfurization.
Background technology
China is the country of SO2 emissions maximum in the world, and sulfur dioxide pollution has made China surpass on 1/3 the area acid rain to occur, become in the world one of three large main Acid Rain Zones.Sulfur dioxide pollution has become the environmental issue of global concern.At present, the input commercial FGD technique of using in the whole world mainly contains: lime stone (lime)-gypsum, flue gas circulating fluidized bed method desulfurization, spray dry desulfurization, the desulfurization of in-furnace calcium spraying flue gas humidification activation method, sea water desulfuration, ammonia process and electronic beam method etc.
Ammonia desulfurizing process is a kind of friendly process, adopts ammoniacal liquor or liquefied ammonia to remove the sulfur dioxide in the flue gas and generate ammonium sulfite as absorbent, and ammonium sulfite also can be used as chemical fertilizer and directly uses, but the less stable of product is difficult to carry, and generally is not accepted; As the paper mill raw materials for production, will produce waste water, cause secondary pollution.And the ammonium sulfate product stable performance wherein contains two kinds of nutrients of nitrogen and sulphur, and is favourable to plant growth, can be as independent fertilizer, and also can be as the raw material of producing compound fertilizer, so the problem of oxidation of ammonium sulfite more and more is subject to people's attention.How efficiently and economically ammonium sulfite being converted into ammonium sulfate is that ammonia desulfurizing process is realized industrialized key.
The oxidizing process of ammonium sulfite namely is the process that ammonium sulfite and combination with oxygen generate ammonium sulfate, the ammonium sulfite of low concentration is easier to oxidation, has higher oxidation rate, but in the higher solution of ammonium sulfite or ammonium sulfate concentrations, the oxidation rate of ammonium sulfite is lower, is subjected to the various factors such as slurry temperature, pH value, O/S ratio, gas-liquid contact area, salinity, oxygen rate of dissolution.
The solution speed of oxygen is higher in the solution, and is more favourable to the oxidation of ammonium sulfite.The solubility of oxygen in water is very little, under the standard state, and 100cm
3Water dissolvable 3.08cm
3Oxygen is 2.08cm in the time of 50 ℃
3In containing the ammonium sulfate solution of high concentration, the viscosity of solution is much larger than water, and solubility and the rate of dissolution of oxygen are lower.How to improve the rate of dissolution of oxygen in containing ammonium sulfate solution and be a difficult problem in the ammonia desulfurizing process.
Contain ammonium sulfate, ammonium sulfite, ammonium bisulfite in the slurries after the desulfurization, wherein ammonium sulfite and ammonium bisulfite are all unstable, if the control of pH value is improper, can exist the escaping of ammonia and sulfur dioxide to escape, environment is produced secondary pollution, how controlling the pH value in the ammonium sulfite slurries oxidizing process, is another difficult problem of the ammonia process of desulfurization.
About ammonium sulfite is direct oxidation into ammonium sulfate, once the someone did kinetics research, and the ammonium sulfite concentration of studying is low, and was generally below 0.1mol/L, unsatisfactory under the high concentration, and ammonium sulfite concentration is very large on the result of the test impact.
Japan had once carried out process exploitation and research to the direct oxidation process of sulphite, and it adopts ammonium sulfite concentration also not high, and ammonium sulfate and ammonium sulfite total salt concentration are about 13%, do not possess industrial application value.
The Li Wei of chemical engineering institute of East China University of Science etc. have tested initial inferior sulfate radical concentration 0.3～0.5mol/L, ammonium sulfate concentrations 0～1.5mol/L.Its experimental result shows that under high concentration, oxidation rate reduces with the increase of inferior sulfate radical concentration, and the ammonium sulfite of high concentration can not be direct oxidation into rapidly ammonium sulfate fully.
The utility model content
The utility model provides a kind of oxidation unit of ammonium sulfite, and ammonium sulfite in the energy Quick Oxidation high-concentration sulfuric acid ammonium salt solution reduces the ammonium sulfate cost recovery, does not exist the escaping of ammonia and sulfur dioxide to escape in the oxidizing process.
A kind of oxidation unit of ammonium sulfite comprises the bottom with the oxidation trough of slurries excavationg pump,
Also comprise:
The ammonification pipeline that is communicated with described oxidation trough top;
Be arranged in the described oxidation trough and be positioned at the oxidation airduct of bottom;
Be arranged on the spaced apart porous plate of some layers in the described oxidation trough and in the middle part of being positioned at.
As preferably, described porous plate is set to 2～5 layers, and every interlamellar spacing is 1～4m, and the aperture of porous plate is 2-20mm, and the hole heart is apart from be 2-5 times of aperture.
As preferably, described oxidation airduct is 0.3-0.6m apart from the distance of oxidation trough bottom.
As preferably, the below of oxidation airduct is provided with several ventholes, and the aperture of described venthole is 3-15mm, and the hole is in the heart apart from be 5-50 times of venthole aperture.
As preferably, described oxidation trough top is provided with blow-down pipe, and described blow-down pipe is provided with air shut-off valve.
As preferably, described oxidation trough top is provided with Pressure gauge.
The ammonium sulfite slurries are entered by the top of oxidation trough after ammoniacal liquor regulates the pH value, under the draft effect of slurries excavationg pump, to the oxidation trough flows.Oxidation air penetrates to the oxidation trough bottom at a high speed through the oxidation airduct of high-pressure oxidation blower fan by oxidation trough bottom, bubble under the effect of buoyancy, move up with solution in the ammonium sulfite catalytic oxidation, generate ammonium sulfate; Oxidation air through some layers of porous plate, with the bubble breaking that rises, increases the oxidation rate that the gas-liquid contact area improves ammonium sulfite under the effect of orifice plate in uphill process.
Regulate the air shut-off valve at oxidation trough top, for increasing the air pressure in the oxidation trough, increased the rate of dissolution of oxygen in solution, guarantee that ammonium sulfite has higher oxidation rate, the ammonium sulfite slurries are Uniform Flow from top to bottom in oxidation trough, slurries flow to oxidation trough when bottom and realize complete oxidation, and oxidation completely ammonium sulfate is delivered to after-treatment system by the slurries excavationg pump and carried out condensing crystallizing, produces highly purified ammonia sulfate crystal.
Described slurries excavationg pump is used for completely ammonium sulfate slurries of flow velocity, the time of staying and the discharge oxidation of control slurries in oxidation trough.The flow of slurries excavationg pump is excessive, and the flow velocity of supplied materials slurries ammonium sulfite slurries in oxidation trough is too fast, and oxidization time is too short, and oxidation is incomplete; Slurries excavationg pump flow is too small, and the slurries oxidization time is long, and the supplied materials slurries cause the waste of cost of investment and operating cost arriving just complete oxidation of oxidation trough middle part.Therefore, as preferably, the flow-control of described slurries excavationg pump should guarantee the time of staying of ammonium sulfite slurries in oxidation trough at 10min-60min, and the flow velocity in oxidation trough is at 10m/h-50m/h.
Described oxidation fan is carried oxidation air by oxidation trough bottom connectivity part to oxidation trough, in order to guarantee that sulfite oxidation is abundant in the slurries, enough tolerance must be arranged, and as preferably, the air quantity of oxidation fan satisfies O/S in the oxidizing process than being 2-5.
Described oxidation airduct is positioned at the oxidation trough bottom, for enough gas-liquid contact areas are arranged between oxidation air and the slurries, the oxidation BOD arranges some equally spaced ventholes, oxidation air penetrates at a high speed through venthole, form the bubble of a large amount of small volumes, effectively raise the oxidation rate of ammonium sulfite.The some airducts that the oxidation airduct can be set to be parallel to each other also can be set to the network structure of some airduct interlaced arrangement.Preferably, the oxidation airduct is positioned at oxidation trough bottom top 0.3m-0.6m, and the pore diameter range of oxidation airduct below venthole is 3mm-15mm, and the hole is in the heart apart from be 5-50 times of venthole aperture.
Described porous plate is positioned at oxidation trough middle part, and oxidation trough is divided into some zones, and effectively anti-oxidation slurries produce eddy current and oxidation is inhomogeneous, and under the separation of some layers of porous plate, the ammonium sulfite slurries are all at the uniform velocity to the oxidation trough flows.The oxidation air bubble that upwards flows bottom oxidation trough is when the pore of process porous plate, and bubble is fractured into less bubble, has increased the gas-liquid contact area, improves the rate of dissolution of oxygen, and the oxidation rate of ammonium sulfite improves rapidly.As preferably, the porous plate in the oxidation trough arranges the 2-5 layer according to the concentration of inferior sulfate radical in the slurries, and every interlamellar spacing is 1m-4m, and the aperture of porous plate is 2mm-20mm, and the hole heart is apart from be 2-5 times of aperture.
Described ammonification pipeline is positioned at the oxidation trough top, ammonification neutralizes before being oxidation, the ammonium sulfite slurries are after ammonification is adjusted to certain pH value, prevent that effectively the escaping of ammonia that produces in the oxidizing process and sulfur dioxide from escaping, as preferably, the ammonium sulfite slurries are 6-8 through the pH value scope of ammonification control.
Described air shut-off valve is positioned on the emptying pipe of oxidation trough outlet, regulating air shut-off valve increases the pressure of oxidation air in the oxidation trough, improve the partial pressure of oxygen of reaction system, promote the oxidation rate of oxygen in slurries, as preferably, the pressure control range at oxidation trough top is 0.01MP-0.3MP.
The beneficial effects of the utility model:
The utility model is regulated its pH value before ammonium sulfite carries out oxidation be 6-8, effectively prevents the escaping of ammonia and the sulfur dioxide escape that produce in the oxidizing process; In the oxidizing process oxidation air is advanced behind the slurries brokenly through porous plate again with stingy blister jet, increase the contact area of oxidation air and inferior sulfate radical, the rate of dissolution of raising oxygen, the oxidation rate of ammonium sulfite improves rapidly.The groove oxygenation efficiency that goes out that adopts technique of the present utility model and device to carry out behind the sulfite oxidation reaches 99.9%, can realize that ammonium sulfate concentrations is not less than the Quick Oxidation of ammonium sulfite in 30% the slurries.
Description of drawings
Fig. 1 is structural representation of the present utility model.
Reference numeral is as follows shown in the figure:
1-oxidation trough 2-oxidation fan 3-porous plate
4-oxidation airduct 5-supplied materials slurries pipeline 6-ammonification pipeline
7-slurries excavationg pump 8-Pressure gauge 9-air shut-off valve.
The specific embodiment
As shown in Figure 1, a kind of oxidation unit of ammonium sulfite, comprise oxidation trough 1, oxidation trough 1 is conventional tank structure, and the bottom of oxidation trough 1 is communicated with a slurries excavationg pump 7, oxidation trough 1 interior layout oxidation airduct 4, oxidation airduct 4 is 0.3～0.6m apart from the distance of oxidation trough 1 bottom, this oxidation airduct 4 can be some that are parallel to each other, and also can be the network structure of some airduct interlaced arrangement, and all airducts are by the external oxidation fan 2 of house steward.
The side of oxidation airduct 4 towards oxidation trough 1 bottom is provided with several equidistant ventholes, and the aperture of this venthole is 3～15mm, and the hole of adjacent venthole is in the heart apart from being 5～50 times of venthole aperture.
Be disposed with from top to bottom some layers of porous plate 3 in the oxidation trough 1, be preferably 2～5 layers, this porous plate 3 becomes some zones with oxidation trough 1 interior separation, and the spacing between the adjacent two layers porous plate 3 is 1～4m, the aperture of porous plate 3 is 2～20mm, and the hole is in the heart apart from being 2～5 times of aperture.
The top of oxidation trough 1 is provided with the slurries entrance, and this slurries entrance is communicated with supplied materials slurries pipeline 5, and ammonification pipeline 6 is connected on the supplied materials slurries pipeline 5, sends at the ammonium sulfite slurries that oxidation trough 1 is front to carry out the pH value to slurries and regulate; The top of oxidation trough 1 also offers drain, and this drain is communicated with emptying exhausting pipeline, and air shut-off valve 9 is set on this exhausting pipeline, and the top of oxidation trough 1 also is provided with Pressure gauge 8.
Technological process of the present utility model is as follows:
Ammonium sulfite slurries after the desulfurization (being the supplied materials slurries) are sent into the oxidation trough 1 from the top of oxidation trough 1 through supplied materials slurries pipeline 5, in supplied materials slurries pipeline 5, after adding ammoniacal liquor adjusting pH value, ammonification pipeline 6 enters oxidation trough 1 by the top, because the supplied materials slurries contain ammonium sulfate, ammonium sulfite, the components such as ammonium bisulfite, wherein ammonium sulfite and ammonium bisulfite are all unstable, if the control of pH value is improper, in the air blast oxidizing process, can exist the escaping of ammonia and sulfur dioxide to escape, environment is produced secondary pollution, pH value by ammonification pipeline slip liquid in future is controlled at 6-8, can well avoid the escaping of ammonia and sulfur dioxide to escape.
The supplied materials slurries enter after the oxidation trough 1, under the draft and the effect of slurries self gravitation of slurries excavationg pump 7, slowly at the uniform velocity to oxidation trough 1 flows, the some layers of porous plate 3 that arrange in the oxidation trough 1 prevent that effectively eddy current from appearring in slurries, in the present embodiment, porous plate 3 in the oxidation trough 1 arranges the 2-5 layer according to the concentration of inferior sulfate radical in the slurries, and every interlamellar spacing is 1m-4m.
Oxidation air is sent into the oxidation airduct 4 of oxidation trough 1 bottom through oxidation fan 2, the high fast direction oxidation trough of venthole through peroxidating airduct 4 bottoms 1 bottom, producing a large amount of minute bubbles moves up under buoyancy, fully contact with the slurries that flow downward, oxidation, the jet action of venthole has increased the gas-liquid contact area, improves the rate of dissolution of oxygen in solution.
Bubble after the venthole jet is gone out is in uphill process, because reducing and each other enrichment of pressure, it is large that the bubble of oxidation air can become gradually, the gas-liquid contact area can reduce gradually, when bubble becomes large process porous plate 3, under the fragmentation of pore, air pocket regenerates the bubble of smaller size smaller, porous plate 3 places and slurries because convection current produces violent disturbance Quick Oxidation.
In order to guarantee that slurries have enough time of staying to finish oxidation in oxidation trough 1, the time of staying of supplied materials slurries in oxidation trough 1, the flow velocity in oxidation trough 1 was at 10m/h-50m/h at 10min-60min; In order to guarantee the oxygenation efficiency of slurries in oxidation trough 1, oxidation airduct 4 is positioned at top, oxidation trough 1 bottom 0.3m-0.6m, the pore diameter range of oxidation airduct 4 below ventholes is 3mm-15mm, the hole is in the heart apart from the 5-50 times that be the venthole aperture, the aperture of porous plate 3 is 2mm-20mm, and heart distance in hole is 2-5 times of aperture.
In order to accelerate the dissolution velocity of oxygen in solution, reduce simultaneously and even eliminate the diffusional resistance of oxygen in solution, effective method has two, one, improves the rate of dissolution of oxygen by the oxygen partial pressure that increases oxidation air; The 2nd, by increasing the gas-liquid contact area, improve the rate of dissolution of oxygen.Establish Pressure gauge 8, establish air shut-off valve 9 at the oxidation air outlet conduit at oxidation trough 1 top exit, increase the pressure of oxidation trough 1 interior oxidation air, improve partial pressure of oxygen, the pressure at oxidation trough 1 top is controlled at 0.01MP-0.3MP.
Embodiment 1
Certain sintering plant, 2 260m
2The sintering flue gas ammonia method desulfurizing engineering adopts this oxidation technology, SO in the flue gas
2Concentration is 2316mg/m
3, oxidation trough entrance slurry pH value is controlled at 7.0, and the flow velocity of slurries in oxidation trough is 40m/h, the O/S ratio of oxidation wind is controlled at 3, and the oxidation airduct aperture of giving vent to anger is 8mm, porous plate spacing 2.0m, 2 layers of porous plate aperture are 10mm, and the hole heart is apart from 30mm, and the oxidation trough top pressure is controlled at 0.05MP.It is 99.8% that slurries go out the groove oxygenation efficiency, and ammonium sulfate concentrations is 33.7% in the oxidation rear slurry.
Certain steam power plant, 2 135WM unit flue gas ammonia method desulfurizing engineerings adopt this oxidation technology, SO in the flue gas
2Concentration is 3560mg/m
3, oxidation trough entrance slurry pH value is controlled at 7.1, and the flow velocity of slurries in oxidation trough is 45m/h, the O/S ratio of oxidation wind is controlled at 3, and the oxidation airduct aperture of giving vent to anger is 10mm, porous plate spacing 2.0m, 3 layers of porous plate aperture are 10mm, and the hole heart is apart from 40mm, and the oxidation trough top pressure is controlled at 0.05MP.It is 99.9% that slurries go out the groove oxygenation efficiency, and ammonium sulfate concentrations is 32.6% in the oxidation rear slurry.
Certain power plant for self-supply, 1 410t/h process of desulfurization for boiler flue gas engineering adopts this oxidation technology, SO in the flue gas
2Concentration is 1830mg/m
3, oxidation trough entrance slurry pH value is controlled at 7.0, and the flow velocity of slurries in oxidation trough is 50m/h, the O/S ratio of oxidation wind is controlled at 3, and the oxidation airduct aperture of giving vent to anger is 10mm, porous plate spacing 2.0m, 2 layers of porous plate aperture are 10mm, and the hole heart is apart from 35mm, and the oxidation trough top pressure is controlled at 0.05MP.It is 99.9% that slurries go out the groove oxygenation efficiency, and ammonium sulfate concentrations is 33.7% in the oxidation rear slurry.
Claims (6)
1. the oxidation unit of an ammonium sulfite comprises that the bottom with the oxidation trough of slurries excavationg pump, is characterized in that,
Also comprise:
The ammonification pipeline that is communicated with described oxidation trough top;
Be arranged in the described oxidation trough and be positioned at the oxidation airduct of bottom;
Be arranged on the spaced apart porous plate of some layers in the described oxidation trough and in the middle part of being positioned at.
2. oxidation unit according to claim 1 is characterized in that, described porous plate is set to 2～5 layers, and every interlamellar spacing is 1～4m, and the aperture of porous plate is 2-20mm, and heart distance in hole is 2-5 times of aperture.
3. oxidation unit according to claim 2 is characterized in that, described oxidation airduct is 0.3-0.6m apart from the distance of oxidation trough bottom.
4. oxidation unit according to claim 3 is characterized in that, the below of oxidation airduct is provided with several ventholes, and the aperture of described venthole is 3-15mm, and the hole is in the heart apart from the 5-50 times that be the venthole aperture.
5. oxidation unit according to claim 1 is characterized in that, described oxidation trough top is provided with blow-down pipe, and described blow-down pipe is provided with air shut-off valve.
6. oxidation unit according to claim 1 is characterized in that, described oxidation trough top is provided with Pressure gauge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320181977 CN203244957U (en) | 2013-04-11 | 2013-04-11 | Oxidation device of ammonium sulfite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320181977 CN203244957U (en) | 2013-04-11 | 2013-04-11 | Oxidation device of ammonium sulfite |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203244957U true CN203244957U (en) | 2013-10-23 |
Family
ID=49371423
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320181977 Expired - Lifetime CN203244957U (en) | 2013-04-11 | 2013-04-11 | Oxidation device of ammonium sulfite |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203244957U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103212348A (en) * | 2013-04-11 | 2013-07-24 | 浙江天蓝环保技术股份有限公司 | Ammonium sulfite oxidation process and device |
-
2013
- 2013-04-11 CN CN 201320181977 patent/CN203244957U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103212348A (en) * | 2013-04-11 | 2013-07-24 | 浙江天蓝环保技术股份有限公司 | Ammonium sulfite oxidation process and device |
| CN103212348B (en) * | 2013-04-11 | 2016-04-06 | 浙江天蓝环保技术股份有限公司 | A kind of oxidation technology of ammonium sulfite and device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201912884U (en) | Ammonia desulfurizer with two-level gas distributors | |
| CN103212348B (en) | A kind of oxidation technology of ammonium sulfite and device | |
| CN102755827B (en) | Flue gas desulfurization process and device adopting acetylene sludge-gypsum method | |
| CN102850092B (en) | Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof | |
| WO2011140820A1 (en) | Wet flue gas desulfurization absorption tower for power plant | |
| CN103191785A (en) | Energy-saving and synergizing wet desulfurization catalyst and using thereof | |
| CN103223292A (en) | Ammonia process flue gas treatment method for acidic tail gas and device | |
| CN101445290A (en) | Environment-friendly high-performance waste water ammonia-removal process and device thereof | |
| CN110479077A (en) | A kind of ammonia process of desulfurization oxidation unit and method | |
| CN103203175B (en) | Flue gas desulfurization and denitration process and device for recovering ammonium sulfate | |
| CN103058435A (en) | Method for circularly processing hot boiler flue gas and desulfurization wastewater | |
| CN105056747A (en) | Process and device for removing SO2 from exhaust gas generated by sulfuric acid production in phosphate chemical enterprise | |
| CN102631837B (en) | Integrated type sulfur-containing waste gas purifying device | |
| CN102824824A (en) | Amino wet combined desulfurization and denitration device and process | |
| CN203244957U (en) | Oxidation device of ammonium sulfite | |
| CN206897143U (en) | A kind of double tower Two-way Cycle lime stone and gypsum wet flue gas desulfurizing system | |
| CN109589750A (en) | Fluorine technique is gone in a kind of economical desulfurization of aluminium electrolytic flue | |
| CN201669053U (en) | Desulfurizing device with gas fume washing component | |
| CN202751947U (en) | Flue gas desulfurization (FGD) device using carbide slag-gypsum method | |
| CN102527223A (en) | Sintering machine flue gas desulfurization process and device thereof | |
| CN203090748U (en) | Oxidation air supply device for desulfurization tower | |
| CN101549253A (en) | Mixed-flow discharge gas treatment method and treatment method | |
| CN206285704U (en) | A kind of utilization paper white sludge is the wet flue gas desulfurizer of raw material | |
| CN104069723A (en) | Combined method for desulfurization, denitration and decarburization of exhaust gas | |
| CN216136981U (en) | Sectional counter-flow type boiler flue gas desulfurization device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20131023 |