CN202193626U - Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization - Google Patents
Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization Download PDFInfo
- Publication number
- CN202193626U CN202193626U CN2011203249978U CN201120324997U CN202193626U CN 202193626 U CN202193626 U CN 202193626U CN 2011203249978 U CN2011203249978 U CN 2011203249978U CN 201120324997 U CN201120324997 U CN 201120324997U CN 202193626 U CN202193626 U CN 202193626U
- Authority
- CN
- China
- Prior art keywords
- evaporative
- diameter
- flue gas
- absorber portion
- oxidation panel
- 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.)
- Withdrawn - After Issue
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 25
- 239000003337 fertilizer Substances 0.000 title claims abstract description 16
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title abstract description 18
- 229910052921 ammonium sulfate Inorganic materials 0.000 title abstract description 18
- 235000011130 ammonium sulphate Nutrition 0.000 title abstract description 18
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 18
- 230000023556 desulfurization Effects 0.000 title abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 22
- 230000008020 evaporation Effects 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 238000001035 drying Methods 0.000 claims abstract description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 34
- 239000003546 flue gas Substances 0.000 claims description 34
- 230000003647 oxidation Effects 0.000 claims description 32
- 238000007254 oxidation reaction Methods 0.000 claims description 32
- 238000002425 crystallisation Methods 0.000 claims description 29
- 230000008025 crystallization Effects 0.000 claims description 28
- 239000002002 slurry Substances 0.000 claims description 26
- 239000006096 absorbing agent Substances 0.000 claims description 19
- 238000005507 spraying Methods 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 14
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- JZRWCGZRTZMZEH-UHFFFAOYSA-N Thiamine Natural products CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N JZRWCGZRTZMZEH-UHFFFAOYSA-N 0.000 claims description 9
- 239000003595 mist Substances 0.000 claims description 9
- KYMBYSLLVAOCFI-UHFFFAOYSA-N thiamine Chemical compound CC1=C(CCO)SCN1CC1=CN=C(C)N=C1N KYMBYSLLVAOCFI-UHFFFAOYSA-N 0.000 claims description 9
- 229960003495 thiamine Drugs 0.000 claims description 9
- 235000019157 thiamine Nutrition 0.000 claims description 9
- 239000011721 thiamine Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000005273 aeration Methods 0.000 claims description 4
- 238000013459 approach Methods 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 13
- 238000012856 packing Methods 0.000 abstract description 5
- 230000002745 absorbent Effects 0.000 abstract 1
- 239000002250 absorbent Substances 0.000 abstract 1
- 230000014759 maintenance of location Effects 0.000 abstract 1
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 239000002562 thickening agent Substances 0.000 abstract 1
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 13
- 239000000243 solution Substances 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 10
- 239000000047 product Substances 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 8
- 239000013078 crystal Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 238000009826 distribution Methods 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 239000012452 mother liquor Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000009987 spinning Methods 0.000 description 3
- 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 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000004567 concrete Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 230000005619 thermoelectricity Effects 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 239000001166 ammonium sulphate Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Inorganic materials [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- ZOMBKNNSYQHRCA-UHFFFAOYSA-J calcium sulfate hemihydrate Chemical compound O.[Ca+2].[Ca+2].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZOMBKNNSYQHRCA-UHFFFAOYSA-J 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000011507 gypsum plaster Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000009856 non-ferrous metallurgy Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a device for producing ammonium sulfate fertilizer by ammonia flue desulfurization , which comprises a desulfurization tower, an evaporation crystallizer, a swirler, a thickener, a centrifugal machine, a drying machine and a packing machine. A stirrer is arranged at the top of the evaporation crystallizer, extending depth of a propeller is 1/3 to 2/3 of the evaporation crystallizer, a cylindrical baffle is arranged on the upper portion of the evaporation crystallizer, and diameter of the cylindrical baffle is 1/3 to 2/3 of the diameter of the evaporation crystallizer. A guide cylinder is arranged in the cylindrical baffle, the diameter of the guide cylinder is 1/3 to 2/3 of the cylindrical baffle, the lower portion of the guide cylinder is located on the upper portion of the swirler of the stirrer, an opening at the upper end of the cylindrical baffle is connected with a vacuum pump, the stirrer, and the cylindrical baffle and the guide cylinder enable crystalline liquid to flow in circulating mode. Retention time of ammonium sulfate particles in the crystalline liquid is prolonged to enable the particles to grow gradually. The diameter of the ammonium sulfate particles is 100-1000 mu m, and the device has the advantages of purifying flue highly, effectively improving utilization rate of ammonia absorbent and the like, thereby saving equipment investment and operating expense.
Description
Technical field
The utility model relates to the flue gas desulfurization technique field in coal-fired thermoelectricity, coal firing boiler, steel sintering machine, nonferrous metallurgy and chemical building material field, relates in particular to the device that a kind of ammonia type flue gas desulfurizing is produced ammonium sulfate fertilizer.
Background technology
Along with the industriallization and the economic construction of China are fast-developing, the pollution problem of SO2 is but serious day by day in the industrial smoke that brings with it.At present; Through large-scale flue-gas desulfurizing engineering construction the Eleventh Five-Year Plan period, the flue gas desulfurization ability and the installed capacity of China have leapt to the No. 1 in the world, still; By 2010; The SO2 that China discharges in atmosphere every year still surpasses 2,000 ten thousand tons, and along with the demand of China's Economic development to the energy and resource, emission source continues to increase.Therefore, in " 12 " and longer afterwards time, the task of China's control SO2 discharging and energy-saving and emission-reduction is still very heavy, exists bigger desulphurization market.
China is with the country of coal as main energy sources, and annual China thermoelectricity, iron and steel, chemical industry, non-ferrous metal and building material industry have discharged a large amount of SO2 in atmosphere, and it is more and more serious to make that atmospheric sulfer pollutes.Simultaneously, China is large agricultural country, needs a large amount of chemical fertilizer every year, therefore from building the angle of resource-conserving, environmentally friendly society, greatly develops green economy, recycling economy, realizes the inevitable choice that becomes of Sustainable development.Simultaneously, further examine the development of China's flue gas desulfurization industry closely, active development new technology, optimisation technique kind and the engineering ratio that puts into operation is the new problem that China's flue gas desulfurization industry is faced.
At present; Domestic employing lime/lime stone-gypsum wet flue gas desulfurizing technology of taking off almost accounts for 90% of whole industry; Though this technology has realized maximization; But have problems such as fouling obstruction, by product gypsum are difficult to handle, discharging CO2, and China is plaster of paris big producing country, the desulfurated plaster of stacking is prone to cause secondary pollution because of utilization ratio is low.And but the ammonia type flue gas desulfurizing technology is as the sulfur removal technology technology of a kind of resource utilization that can in desulfurization, obtain the high added value thiamine fertilizer; Have advantages such as desulfurization is efficient, producing ammonium sulfate byproduct chemical fertilizer, floor space is little, investment is relatively little simultaneously; Be fit to China's national situation; Obtained paying close attention to widely and using, but realized the resource circulation recycling.
Traditional ammonia flue gas desulfurization technique mainly contains: the absorption of (1) collection, oxidation, concentrated, the incorporate crystallization inside tower technology of crystallization; (2) absorption, oxidation and evaporative crystallization technique concentrated, the crystallization separate operation.Adopt (1) to plant crystallization inside tower technology; The heat that can effectively utilize former flue gas carries out heat exchange with the desulphurization circulating liquid concentrator; Moisture constantly evaporates in the sulphur ammonium slurries thereby make; Until forming xln, the slurries that contain xln then obtain ammonium sulfate products through follow-up spinning of sulphur ammonium and drying plant again.Therefore this kind technology have bigger advantage owing to can effectively utilize the heat of former flue gas aspect energy-conservation, but less through the ammonium sulfate particle diameter of this kind technology formation; Distribution range is narrower; Sulphur ammonium particle grain size distribution has only 30-60 μ m, has caused the difficulty of follow-up spinning, is not easy to obtain qualified ammonium sulfate product; And output is very low, causes rate of breakdown very high simultaneously.Adopt (2) to plant evaporative crystallization technique, the sulphur ammonium particle that obtains is bigger, and size distribution is more even, and the ammonium sulfate products quality that obtains is better, and rate of breakdown is low; But adopt this kind technology but to need the steam energy of labor, increased corresponding running cost.
The utility model content
The technical problem that the utility model will solve is: in order to overcome the problem that traditional ammonia desulfuration equipment exists, improve the technical and economic performance of desulfurization and recycling comprehensively, provide a kind of ammonia type flue gas desulfurizing to produce the device of thiamine fertilizer.
The utility model solves the technical scheme that its technical problem adopted: a kind of ammonia type flue gas desulfurizing is produced the device of thiamine fertilizer; Comprise thionizer, evaporative crystallizer, swirler-, stiff device, whizzer, drying machine and wrapping machine; From top to bottom for demist section, absorber portion, evaporative crystallization section and oxidation panel, be provided with dividing plate between evaporative crystallization section and the oxidation panel in the thionizer, demist section top is provided with exhanst gas outlet; Absorber portion is provided with 2-4 level absorber portion spraying layer; The evaporative crystallization section is provided with gas approach and evaporator section spraying layer, and oxidation panel is provided with compressed air inlet and liquefied ammonia injection tube, and the outlet of absorber portion phegma is connected with oxidation panel through pipeline; Oxidation panel links to each other with the absorber portion spraying layer through slurry circulating pump, and evaporative crystallizer links to each other with the evaporative crystallization section with oxidation panel with slush pump through pipeline; The swirler-opening for feed links to each other with the evaporative crystallizer discharge port; Swirler-, stiff device, whizzer, drying machine link to each other through pipeline with wrapping machine successively; It is characterized in that: said evaporative crystallizer is the negative pressure evaporation mold; The evaporative crystallizer top is provided with whisking appliance, and whisking appliance is a propeller type, water screw go deep into the 1/3-2/3 that the degree of depth is an evaporative crystallizer; Evaporative crystallizer top is provided with drum shape baffle plate; Drum shape baffle plate diameter is the 1/3-3/4 of evaporative crystallizer diameter; Be provided with guide shell in the drum shape baffle plate, draft tube diameter is the 1/3-2/3 of drum shape baffle plate diameter, and the guide shell bottom is positioned at the top of agitator propeller; Drum shape baffle plate open upper end is connected with vacuum pump through pipeline.
Described demist section is provided with the two-stage baffle type mist eliminator and has automatic flushing device, and spacing is 1.0-2.0m between the two-stage mist eliminator, and mist eliminator is topmost apart from exhanst gas outlet 1-3m, and mist eliminator is bottom apart from last layer absorber portion spraying layer 1-3m.
Said thionizer oxidation panel middle and upper part is provided with two stages of compression air gas sparger; The oxidation panel bottom is provided with the sidewall whipping appts in the scope of 0.5-2m at the bottom of the tower; Sidewall whipping appts top is provided with the oxidation air aeration tube, and oxidation air aeration tube lower end is provided with solarization air cap, and the aperture is 1-10mm.
Described absorber portion spraying layer and evaporative crystallization section spraying layer are provided with liquid distributor, and liquid distributor is a spiral awl nozzle.
The beneficial effect of the utility model is: adopt a kind of ammonia type flue gas desulfurizing of the present invention to produce the device of ammonium sulfate fertilizer; The slurries of the heat that can effectively utilize former flue gas after to absorbing sulfur dioxide carry out evaporating, concentrating and crystallizing; Adopt novel negative pressure evaporation mold further slurries to be concentrated simultaneously; In the negative pressure evaporation mold, adopting a series of device to make sulphur ammonium particle can have time enough simultaneously further grows up; Thereby effectively overcome the too small problem of formed sulphur ammonium grain diameter in traditional ammonia process saturated crystallization technology, avoided causing the difficulty of follow-up spinning and the damage of equipment because of sulphur ammonium particle diameter is too small; Since the heat of the former flue gas that makes full use of to slurries conduct heat, transpiring moisture; Thereby overcome the problem of a large amount of steam of traditional ammonia process evaporative crystallization technique consumption; And the doctor solution that absorbs and do not contain solid particulate basically of being used to circulate by the circulation crystal solution that the negative pressure evaporation mold pumps into thionizer evaporative crystallization section; Greatly reduce wearing and tearing and corrosion, strengthened its wearing quality greatly, saved facility investment indirectly slurry circulating pump and evaporative crystallization circulating pump impeller.In the negative pressure evaporation mold; Sulphur ammonium small-particle has enough residence time one-tenth and grows up to bigger sulphur ammonium particle, and through series of processes such as separation, drying, packings, it is even finally to obtain size distribution; The ammonium sulfate products that quality is good, but realize changing by the resource utilization of sulphur to thiamine fertilizer.
Through novel process and apparatus processes that a kind of efficient energy-saving ammonia type flue gas desulfurizing of the present invention is produced ammonium sulfate fertilizer, the decreasing ratio of main acid, alkaline pollutant and flue dust can reach in the flue gas: SO
2:>=95.5%; SO
3:>=98%; NOx>=35%; HX (X:F, Cl)>=95%; Flue dust:>=70%; The escaping of ammonia≤8mg/Nm
3The size distribution 100-1000 μ m of ammonium sulfate products; Therefore have the high purification flue gas, efficiently remove SO
2And other harmful sour gas, effectively improve characteristics such as ammonia absorption agent utilization ratio, and save facility investment and working cost simultaneously, have bigger practical applications and industrialization value.
Description of drawings
Fig. 1 is the utility model structural representation.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further specified.
As shown in Figure 1; Flue gas from coal-burning installation enters into tower through the gas approach 101 that is positioned at thionizer 1 evaporative crystallization section 113; Pump into evaporator section spraying layer 14 at evaporative crystallization section 113 and slurries through evaporative crystallization recycle pump 33, after liquid distributor is uniformly distributed with, carries out counter current contact and conduct heat from the evaporative crystallizer settling section; Realization moisture evaporation, slurries are carried dense, and the temperature of slurries also will be heated to 40-80 ℃ simultaneously; Flue gas behind the decreasing temperature and increasing humidity enters into absorber portion 112 through the gas-liquid distributor that is positioned at 112 of evaporative crystallization section 113 and absorber portions; In absorber portion 112; The desulfurization slurry counter current contact that flue gas and the liquid distributor on absorber portion spraying layer 13 are uniformly distributed with from oxidation panel 114; Make in sulfur in smoke and the slurries the sweetening substance rapid reaction and realize desulfurization; The unlatching progression of concrete spray equipment is confirmed according to exhaust gas volumn and sulphur content, controls through the unlatching platform number of slurry circulating pump 31; , guarantee simultaneously less than 8mg/Nm in order to reduce entrained ammonia amount in the flue gas after the desulfurization
3, be provided with one deck packing layer 12 at the topmost of oxidation panel, and above this packing layer, be provided with automatic flushing device.Flue gas passes packing layer afterwards to the demist section 111 that is positioned at thionizer top; In the demist section, be provided with two-stage baffle type mist eliminator 11; The entrained size droplet diameter of desulfurization flue gas is greater than the particulate of 15 μ m; Collision through between flue gas and traverse baffle all is able to away, guarantees that finally water cut after flue gas is through the demist section is less than 75mg/Nm
3Finally exhanst gas outlet 102 dischargings of flue gas through the demist section through being positioned at the thionizer top.
As shown in Figure 1, the desulfurization absorption liquid of absorber portion 112 bottoms is connected through the top of pipe gravity flow pipeline with oxidation panel 114, and phegma is main with ammonium bisulfite mainly; And through discovering; Therefore the real ammonium sulphite that is mainly of participating in absorption reaction in the doctor solution, is ammonium sulphite through the mode that adds liquefied ammonia to oxidation panel with the ammonium bisulfite neutralization; Consider the unstable of ammonium sulphite and the purposes of product simultaneously; Logical compressed-air actuated mode is an ammonium sulfate with the part sulfite oxidation in absorption liquid through adopting in decision, is provided with special pressurized air gas distributor 16 at oxidation panel 114, and the ingress of pressurized air gas distributor is connected with the pressurized air blower fan through compressed air line; And be provided with special ammonification point in the corresponding position of pneumatic line; Concrete ammonia residual is regulated according to the pH value of mother liquor in the tower, and the pH value of mother liquor is controlled at 5.5-6.0, because absorption liquid has higher relatively sulfurous gas uptake rate in this pH value scope.Simultaneously for desulphurization mother solution is mixed; Improve compressed-air actuated utilization ratio; Oxidation panel apart from its bottom 0.5-2m scope in, be uniformly distributed with 3-6 platform sidewall whipping appts 17, make the ammonium sulfite solution of generation can be oxidized to ammoniumsulphate soln fast; Guaranteed that rate of oxidation reaches more than 97%, the density of whole mother liquor remains on 1.05g/cm simultaneously
3To 1.18g/cm
3Between, concentration is controlled in 35%.
As shown in Figure 1, the serum density when oxidation panel 114 bottoms reaches 1.12g/cm
3To 1.18g/cm
3The time, slurries are driven into the top of evaporative crystallizer 2 through mother liquor overboard pump 32, when the liquid level in the evaporative crystallizer reaches certain value and gets; Open evaporative crystallization recycle pump 33, will between evaporative crystallizer 2 and drum shape baffle plate 22, be driven into thionizer evaporator section spraying layer by the slurries in the settling section, after liquid distributor is uniformly distributed with, contact with former flue gas adverse current; Carry out gas-liquid heat-transfer, moisture evaporation, slurries are concentrated, the crystal solution of evaporative crystallization section is through the pipe gravity flow pipeline between evaporative crystallization section and evaporative crystallizer; Flow into the lower region of negative pressure evaporation mold by the lower end of evaporative crystallization section; Unlatching is positioned at the propeller type stirrer 21 at evaporative crystallizer top, makes crystal solution along guide shell 23 moved upward inside through stirring, overflows from the guide shell top then to enter into drum shape baffle plate 22 zones; Final slurries are along the regional bottom of freely falling back to the negative pressure evaporation mold between guide shell 23 and the drum shape baffle plate 22; In this process, through stirring crystal solution is mixed, overcome the liquid-film resistance of nucleating surface; Make sulphur ammonium molecule can be diffused rapidly to nucleating surface; Make sulphur crystalline ammonium body in crystal solution, be suspended state simultaneously, prolong the residence time of particle in crystal solution, have enough one-tenth long-time sulphur ammonium nucleus.
Upper surface perforate at negative pressure evaporation mold drum shape baffle plate links to each other with vacuum pump, vacuumizes through vacuum pump, and keeping the vacuum tightness in the negative pressure evaporation mold is 20-80kpa; In this vacuum tightness, low under the relative normal pressure of the saturated vapor pressure of water vapor, moisture more is prone to evaporation; Can further carry slurries dense, and according to the practical situation of slurries, the opening degree of decision vacuum pump; Thereby the degree of super saturation of control slurries; In the steady district of Jie who strength of solution is in be easy to sulphur ammonium solute nucleation, grow up, finally obtain sulphur crystalline ammonium particle grain size distribution scope, reduced technical requirements whizzer at 100 μ m-1000 μ m; Reduced the failure rate of centrifugation apparatus simultaneously, and made the quality that obtains ammonium sulfate products better.
As shown in Figure 1, and the circulation that is positioned at the absorption tower oxidation panel absorbs slurries and belongs to unsaturated solution, does not contain solid particulate, greatly reduces the technical requirements to the slurry circulating pump material; And the slurries in the settling section also contain the solid particulate of very small amount between negative pressure evaporation mold 2 and drum shape baffle plate 22, so effectively reduce the wearing and tearing of desulfurization crystal solution to the crystallisation cycle pump impeller, improve the work-ing life of equipment, have saved investment indirectly.
As shown in Figure 1, when the mass concentration of slurries in the negative pressure evaporation mold reaches 10%-30%, open sulphur crystalline ammonium liquid overboard pump 34; The crystal solution that will be positioned at negative pressure evaporation mold bottom is transported to the opening for feed of swirler-3, and after swirler-3 initial gross separations, the mass concentration of slurries reaches 40%-65% in the underflow case; The swirler-underflow opening links to each other with the stiff device, and the stiff device links to each other with refrigerating unit, and liquid concentrator is fully cooled off; Sulphur ammonium particle is further grown up, then by the stiff device through the opening for feed of pipe-line transportation, after whizzer separates to whizzer 4; Obtain water cut less than 5% the thick product of sulphur ammonium,, enter into drying machine 5 then through the whizzer feed opening; Drying machine can be vibrated fluidized bed formula drying machine or cylindrical drier here, and less than 1%, dry good sulphur ammonium material is finally packed through wrapping machine 7 through the dried sulphur ammonium of drying machine material moisture; Obtain qualified ammonium sulfate products, but realize resource utilization production.
Claims (4)
1. an ammonia type flue gas desulfurizing is produced the device of thiamine fertilizer; Comprise thionizer, evaporative crystallizer, swirler-, stiff device, whizzer, drying machine and wrapping machine; From top to bottom for demist section, absorber portion, evaporative crystallization section and oxidation panel, be provided with dividing plate between evaporative crystallization section and the oxidation panel in the thionizer, demist section top is provided with exhanst gas outlet; Absorber portion is provided with 2-4 level absorber portion spraying layer; The evaporative crystallization section is provided with gas approach and evaporator section spraying layer, and oxidation panel is provided with compressed air inlet and liquefied ammonia injection tube, and the outlet of absorber portion phegma is connected with oxidation panel through pipeline; Oxidation panel links to each other with the absorber portion spraying layer through slurry circulating pump, and evaporative crystallizer links to each other with the evaporative crystallization section with oxidation panel with slush pump through pipeline; The swirler-opening for feed links to each other with the evaporative crystallizer discharge port; Swirler-, stiff device, whizzer, drying machine link to each other through pipeline with wrapping machine successively; It is characterized in that: said evaporative crystallizer is the negative pressure evaporation mold; The evaporative crystallizer top is provided with whisking appliance, and whisking appliance is a propeller type, water screw go deep into the 1/3-2/3 that the degree of depth is an evaporative crystallizer; Evaporative crystallizer top is provided with drum shape baffle plate; Drum shape baffle plate diameter is the 1/3-3/4 of evaporative crystallizer diameter; Be provided with guide shell in the drum shape baffle plate, draft tube diameter is the 1/3-2/3 of drum shape baffle plate diameter, and the guide shell bottom is positioned at the top of agitator propeller; Drum shape baffle plate open upper end is connected with vacuum pump through pipeline.
2. a kind of ammonia type flue gas desulfurizing according to claim 1 is produced the device of thiamine fertilizer; It is characterized in that: described demist section is provided with the two-stage baffle type mist eliminator and has automatic flushing device; Spacing is 1.0-2.0m between the two-stage mist eliminator; Mist eliminator is topmost apart from exhanst gas outlet 1-3m, and mist eliminator is bottom apart from last layer absorber portion spraying layer 1-3m.
3. a kind of ammonia type flue gas desulfurizing according to claim 1 is produced the device of thiamine fertilizer; It is characterized in that: said thionizer oxidation panel middle and upper part is provided with two stages of compression air gas sparger; The oxidation panel bottom is provided with the sidewall whipping appts in the scope of 0.5-2m at the bottom of the tower; Sidewall whipping appts top is provided with the oxidation air aeration tube, and oxidation air aeration tube lower end is provided with solarization air cap, and the aperture is 1-10mm.
4. a kind of ammonia type flue gas desulfurizing according to claim 1 is produced the device of thiamine fertilizer, and it is characterized in that: described absorber portion spraying layer and evaporative crystallization section spraying layer are provided with liquid distributor, and liquid distributor is a spiral awl nozzle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203249978U CN202193626U (en) | 2011-08-31 | 2011-08-31 | Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203249978U CN202193626U (en) | 2011-08-31 | 2011-08-31 | Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202193626U true CN202193626U (en) | 2012-04-18 |
Family
ID=45948547
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011203249978U Withdrawn - After Issue CN202193626U (en) | 2011-08-31 | 2011-08-31 | Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202193626U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102850092A (en) * | 2011-08-31 | 2013-01-02 | 上海克硫环保科技股份有限公司 | Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof |
| CN104478514A (en) * | 2014-12-02 | 2015-04-01 | 成都华西堂投资有限公司 | Heat-pump evaporation process for preparing chemical fertilizer from flue gas purification byproducts |
-
2011
- 2011-08-31 CN CN2011203249978U patent/CN202193626U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102850092A (en) * | 2011-08-31 | 2013-01-02 | 上海克硫环保科技股份有限公司 | Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof |
| CN104478514A (en) * | 2014-12-02 | 2015-04-01 | 成都华西堂投资有限公司 | Heat-pump evaporation process for preparing chemical fertilizer from flue gas purification byproducts |
| CN104478514B (en) * | 2014-12-02 | 2017-06-20 | 成都华西堂投资有限公司 | A kind of utilization gas cleaning accessory substance prepares the thermo-compression evaporation technique of chemical fertilizer |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102850092B (en) | Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof | |
| CN101579602B (en) | Energy-saving and high-quality ammonia desulphurization process for ammonia sulfate recovery | |
| CN102847422B (en) | Apparatus for desulfurizing smoke through ammonia process | |
| CN200998639Y (en) | Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower | |
| CN101524620B (en) | Segment-based ammonia method flue gas desulfurization device | |
| CN201454396U (en) | Spray desulfurization tower integrating absorption, oxidation, crystallization, demisting and cooling | |
| CN1408464A (en) | Removing and recovering process and device for SO2 in flue gas | |
| CN101862583B (en) | Flue gas desulfurization process suitable for sintering machine of steel mill | |
| CN201026440Y (en) | Absorption, oxidation, concentration combined desulfurizing tower | |
| CN202823151U (en) | Multistage spray efficient wet process of flue gas desulfurization and synergistic mercury removal integrated device | |
| CN103585877B (en) | Flue gas desulfurization rear slurry is utilized to prepare the system of magnesium sulfate | |
| CN101306317A (en) | Tower top discharge type flue gas desulfurization method | |
| CN112875968B (en) | A desulfurization wastewater zero discharge system and method | |
| CN103203175B (en) | Flue gas desulfurization and denitration process and device for recovering ammonium sulfate | |
| CN102029105A (en) | Double-tower ammonia method desulfuration device and process | |
| CN101862582A (en) | Separation tower type boiler flue gas desulfurization process | |
| CN102205204A (en) | Wet ammonia desulfurization concentration process of cold and hot state discharge | |
| CN103861426B (en) | A kind of flue gas desulfurization and dedusting also reclaims the method for sodium sulfite | |
| CN2799059Y (en) | Inside-crystallizing ammonia-processed desulfurization tower | |
| CN202193626U (en) | Device for producing ammonium sulfate fertilizer by ammonia flue desulfurization | |
| CN101306319A (en) | Direct discharging flue gas treatment method | |
| CN100506351C (en) | A method and device for recovering sulfur dioxide in flue gas to produce ammonium sulfate | |
| CN101549254A (en) | Jacking flue gas processing device and method | |
| CN103601215A (en) | Wet ammonium sulfate product and preparation method thereof | |
| CN203737091U (en) | Device for desulfuration and denitration through ammonia process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20120418 Effective date of abandoning: 20140618 |
|
| RGAV | Abandon patent right to avoid regrant |