CN100335154C - Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process - Google Patents
Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process Download PDFInfo
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- CN100335154C CN100335154C CNB2005100863878A CN200510086387A CN100335154C CN 100335154 C CN100335154 C CN 100335154C CN B2005100863878 A CNB2005100863878 A CN B2005100863878A CN 200510086387 A CN200510086387 A CN 200510086387A CN 100335154 C CN100335154 C CN 100335154C
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- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 39
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 239000003546 flue gas Substances 0.000 title claims abstract description 32
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 28
- 238000007254 oxidation reaction Methods 0.000 title claims description 65
- 230000003647 oxidation Effects 0.000 title claims description 61
- 238000006477 desulfuration reaction Methods 0.000 title claims description 51
- 230000023556 desulfurization Effects 0.000 title claims description 51
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 title abstract 5
- 238000007613 slurry method Methods 0.000 title abstract 3
- 239000007788 liquid Substances 0.000 claims abstract description 52
- 239000002002 slurry Substances 0.000 claims abstract description 37
- 238000005516 engineering process Methods 0.000 claims abstract description 33
- 238000010521 absorption reaction Methods 0.000 claims abstract description 30
- 238000002425 crystallisation Methods 0.000 claims abstract description 19
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims abstract description 18
- 230000008025 crystallization Effects 0.000 claims abstract description 14
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims abstract description 8
- 235000019341 magnesium sulphate Nutrition 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 239000002245 particle Substances 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 239000012535 impurity Substances 0.000 claims description 12
- 239000000843 powder Substances 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 239000012452 mother liquor Substances 0.000 claims description 9
- 230000001376 precipitating effect Effects 0.000 claims description 9
- 239000012141 concentrate Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 229910052717 sulfur Inorganic materials 0.000 claims description 6
- 239000011593 sulfur Substances 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 3
- 229940076230 magnesium sulfate monohydrate Drugs 0.000 claims description 2
- LFCFXZHKDRJMNS-UHFFFAOYSA-L magnesium;sulfate;hydrate Chemical compound O.[Mg+2].[O-]S([O-])(=O)=O LFCFXZHKDRJMNS-UHFFFAOYSA-L 0.000 claims description 2
- 238000011027 product recovery Methods 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 6
- 239000010440 gypsum Substances 0.000 abstract description 3
- 229910052602 gypsum Inorganic materials 0.000 abstract description 3
- 230000001105 regulatory effect Effects 0.000 abstract description 3
- 239000013078 crystal Substances 0.000 abstract description 2
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 abstract 1
- 238000002156 mixing Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 18
- ZGBSOTLWHZQNLH-UHFFFAOYSA-N [Mg].S(O)(O)(=O)=O Chemical compound [Mg].S(O)(O)(=O)=O ZGBSOTLWHZQNLH-UHFFFAOYSA-N 0.000 description 7
- 208000005156 Dehydration Diseases 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- IBBFGFWMAMKXJW-UHFFFAOYSA-N [Mg].S(O)(O)(=O)=O.[Mg] Chemical compound [Mg].S(O)(O)(=O)=O.[Mg] IBBFGFWMAMKXJW-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000010410 dusting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 235000014380 magnesium carbonate Nutrition 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 229940091250 magnesium supplement Drugs 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- SMDQFHZIWNYSMR-UHFFFAOYSA-N sulfanylidenemagnesium Chemical compound S=[Mg] SMDQFHZIWNYSMR-UHFFFAOYSA-N 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The present invention provides technology for desulphurizing magnesium oxide flue gas and reclaiming products by a thick slurry method, which relates to the improvement of the prior art for desulphurizing magnesium oxide flue gas with a wet method and reclaiming products. The present invention is characterized in that thick slurry liquid is separated and led out in the courses of desulphurization of circulating absorption liquid; then, air is blown into the thick slurry liquid; steam is used for heating and regulating temperature to oxidize the thick slurry of the one-time desulphurized product MgSO3 to mixing liquid with the MgSO4 of which the concentration reaches the production level of industrial magnesium sulfate; MgSO4.7H2O with coarse crystal particles is separated through filtration and crystallization. Compared with the prior art, the technology for desulphurizing magnesium oxide flue gas and reclaiming products by a thick slurry method has the advantages of simplicity, reliability and great reduction of reclaiming and utilizing cost. The use value of the reclaimed MgSO4 7H2O is much higher than that of gypsum and MgSO3. From the aspect that desulphurization is carried out without reclaiming, the reclaiming benefit of the magnesium oxide flue gas is not lower than but even superior to that of the production of industrial magnesium sulfate.
Description
Technical field
The invention belongs to flue gas desulfurization and product resource technology field, particularly product MgSO of magnesia desulfurization
3Thick slurry process oxidation and oxidation product MgSO
4Reclaim technology.
Background technology
The wet process of FGD technology is control SO
2The major technique means that discharging and control acid rain pollute.Particularly the flue gas desulfurization of limestone/gypsum method has become the dominant technology of domestic and international boiler flue gas desulfurization.This technology and China abound with that the national conditions of ore cream are incompatible, and the problem that the disposal of desulfurated plaster becomes enterprise's heavy burden appears, and its desulfurization operation expense is also high.Existing problem at the limestone/gypsum method, produce magnesite and as the national conditions of the world's strongest nation of magnesia and magnesium salts production and outlet in conjunction with China is rich, propose a kind of flue gas desulfurization by magnesia wet method and product and reclaimed new technology, also obtained invention patent mandate.Special as contrast technological process of the present invention, as shown in Figure 1.Through flue gas reheat device and the cooling of pre-wash device, enter SO from the sulfur-containing smoke gas behind the boiler dusting
2The absorption tower desulfurization.Flue gas after being purified is sent to smoke stack emission through demist dehydration and hot again the intensification.Desulfurizing agent adopts cheap common magnesia powder, and the slaking slurries that are mixed with high concentration enter SO with circulating absorption solution
2The absorption tower.The MgSO that desulfurization generates
3In the oxidation trough of bottom, absorption tower, in time be oxidized to the MgSO of solubilised state by the air of sending into
4,, generate the MgSO under the desulfurization equilibrium temperature through circulation desulfurization and oxidation and concentration processes
4Saturated or quasi saturation solution; Utilize the heat effect of inlet flue gas to strengthen and raising oxidation trough temperature simultaneously, make MgSO in the absorption liquid
4Concentration near or reach commercial production levels.The absorption liquid of carrying after dense is removed solid impurity after filtration, again through crystallization and centrifugal dehydration realization and liquid phase separate impurities, after low temperature drying makes industrial sulphuric acid magnesium (being epsom salt).Producing industrial sulphuric acid magnesium earlier is the requirement that guarantees product purity and improve crystallization yield.This technology has solved desulfurization master technology preferably and has reclaimed being connected of process matched therewith, provides assurance for reclaiming industrial sulphuric acid magnesium magnesium cost-effectively, thereby significant technology economy advantage is arranged.It directly reclaims industrial products MgSO
47H
2O, rather than the raw material of industry MgSO that reclaimed of U.S.'s magnesia sulfur removal technology
3, do not need thermal decomposition to reclaim SO
2Tediously long technology; And it reclaims technology more simplifies, and does not resemble and reclaims MgSO
3It is complicated like that to make dry powder.Never reclaim the angle that also gets desulfurization and say that as the recovery technology of desulfurization product, its efficiency of investment also obviously is better than or is equal to the production of industrial sulphuric acid magnesium.Although have this advantage, still there is following deficiency as contrast technology of the present invention:
(i) generating plant flue gas lower to exhaust gas temperature, the temperature of its desulfurization absorption liquid is subjected to the restriction of smoke re-heater and reduces the dense level of putting forward.
(ii) lower to sulfur-bearing coal, its desulfurization absorption liquid is proposed the restriction that dense level is subject to systematic water balance.
(iii) put forward the dense power consumption that will strengthen circulating pump, correspondingly require frequency control and increase regulate expenditure.
(iv) sulphur coal flue gas desulfurization is more suitable in recovery, and corresponding oxidation aeration rate will be multiplied.Oxidation in circulation liquid pool (being oxidation trough), because of its liquid measure is big, energy consumption is also big.
(v) the circulation desulfurization process constantly generates new MgSO
3And Mg (HSO
3)
2, both all have not by the equilibrium concentration of oxidation in time and conversion; Once breaking away from circulation, be difficult to oxidation.
(vi) product and impurity are carried densely synchronously, and non-water substance percentage composition is constant substantially in the absorption liquid.
Summary of the invention
The objective of the invention is provides a kind of MgSO at the deficiencies in the prior art and defective
3Thick slurry process oxidation and MgSO
4Reclaim new technology, promptly in the circulation desulfurization process, absorption liquid is not carried out forced oxidation, both helped to improve the utilization rate of surplus oxygen in the flue gas, can facilitate MgSO again
3The crystallization precipitating; Extract concentrated slurry after precipitating forms certain concentration of slurry or through vortex method, or extract underflow out from the circulatory pool bottom by centrifugal pump, emphasis concentrates solid product and liquid phase is formed constant; Again underflow is carried out oxidation, the high concentration MgSO of generation
4Crystallization and dehydration after filtration,, substep realization and solid phase and liquid phase separate impurities, drying is made industrial products again, thereby under investment increase situation seldom, properly settled the problem that existing technology exists, improved the reliability of oxidation and concentration processes greatly, significantly reduce the power consumption of circulating pump and oxidation fan, further improve the technical and economic performance that desulfurization and product thereof reclaim.
Technical solution of the present invention is as follows:
New technology is reclaimed in a kind of magnesia flue gas desulfurization and the oxidation of product thick slurry process, comprises the pre-wash cooling, common magnesia powder preparation desulfurizer slurry, and circulation absorbs SO in the absorption tower
2, demist and flue gas reheat sulfur removal technology step, and desulfurization slurry concentrates oxidation and desulfurization product reclaims technology, it is characterized in that described desulfurization slurry concentrates oxidation and recovery technology is carried out as follows:
1) absorbs SO in circulation
2In the process, utilize surplus oxygen in the flue gas with once desulfurization product MgSO
3Partial oxidation, most of partial crystallization sinks;
2) play the precipitating thing with underflow pump (13) backlash of boosting, extract underflow liquid above near the precipitating layer, the underflow liquid part of proposition is returned the absorption liquid circulatory pool through bypass and is continued to wash away; Another part enters the temperature adjustment oxidation trough, and makes the overflow thin liquid of temperature adjustment oxidation trough return circulatory pool, makes the MgSO in the underflow liquid
3Concentration reaches commercial production levels after oxidation; Or the underflow liquid that proposes is concentrated through eddy flow earlier, and concentrate is introduced temperature adjustment oxidation trough (6) again, and the overflow thin liquid returns circulatory pool;
3) air is blasted the temperature adjustment oxidation trough, make MgSO
3Be oxidized to MgSO
4, and heat temperature adjustment and insulation, prevent MgSO
4Crystallization before crystallizer;
4) slurries after the temperature adjustment oxidation are removed solid impurity after filtration; Cleaner liquid adopts the water cooling crystallization to generate seven water MgSO of mm level
4Coarse grain; Magma is through centrifugal dehydration, and the mother liquor major part after the separation is returned the temperature adjustment oxidation trough; Fraction effluxes to keep the liquid phase impurity level of follow-up crystallization permission;
5) oven dry of the product after will dewatering, the control bake out temperature obtains epsom salt, magnesium sulfate monohydrate or anhydrous magnesium sulfate.
Heating temperature adjustment and being incubated the step 2 of said method) adopts on-site steam directly to heat temperature adjustment and insulation; And being provided with the tangential inlet of underflow liquid in temperature adjustment oxidation trough bottom, the center is provided with the overflow pipe of two kinds of differing heights, underflow liquid is played secondary carry densely, and carries dense again to the mother liquor and the underflow liquid mixed oxidization that return.
Technical characterictic of the present invention also is: described common magnesia powder preparation desulfurizer slurry adopts the circulating absorption solution preparation, distributing a small gangs of absorption liquid from the circulating-pump outlet side tangentially enters and washes away slurry commanding tank bottom, magnesia powder is one side input from the top, particle slurries tiny or refinement are introduced the circulating pump water inlet pipe from the opposite side overflow, are mixed into the absorption tower desulfurization with circulation fluid.
The present invention has compared with prior art kept the basic advantage and the high-lighting progress of contrast technology; Compare with contrast technology, also have the following advantages and improve:
The present invention changes oxidation in time in the circulation desulfurization process into the thick slurry process oxidation, and the equipment investment volume of required increase is very little.The high concentrated absorption solution that flue gas desulfurization can generate only is several m
3/ h, the temperature adjustment oxidation trough capacity of setting up is less than 1/10th even a thirtieth of circulatory pool, and is littler to the influence of desulfurization project gross investment.The MgSO of the main commute precipitating of thick slurry process of the present invention
3Crystal grain is proposed dense oxidation, can propose the high concentration slurries under much lower liquid concentration, is reoxidised into the MgSO of high concentration
4Mixed liquor has fundamentally been got rid of the said system sexual factor to MgSO
4Propose dense interference; Its oxidation processes amount is again little, add and utilize on-the-spot steam the underflow temperature adjustment, put forward better reliability dense and that reclaim thereby make, efficient is higher, it is more guaranteed to reclaim product quality, and can significantly reduce the power consumption of absorption liquid circulation and desulfurization product oxidation, also more help the transformation that engineering has been built in calcium method and the desulfurization of magnesium method.
Description of drawings
Fig. 1 is contrast technology flue gas desulfurization and crystallization reclaim sulfuric acid magnesium process chart.
Fig. 2 is flue gas desulfurization by magnesia wet method provided by the invention and thick slurry process oxidation reclaim sulfuric acid magnesium process chart.
Fig. 3 is the system equipment structural representation of flue gas desulfurization by magnesia wet method provided by the invention and thick slurry process oxidation reclaim sulfuric acid magnesium process implementing example.
Among the figure: the 1-prewashing column; 2-SO
2The absorption tower; The 3-demister; The 4-smoke re-heater; 5-magnesia slurry commanding tank; 6-temperature adjustment oxidation trough; The 7-filter; The 8-cooler crystallizer; The 9-centrifugal dehydrator; The 10-hot-air drier; 11-mother liquor collecting tank; The 12-circulating pump; The 13-underflow pump; 14-mother liquor pump; The 15-oxidation fan.
The specific embodiment
Below in conjunction with accompanying drawing the present invention is specified.
As shown in Figures 2 and 3, from the boiler sulfur-containing smoke gas behind the electric precipitation, after 4 coolings of flue gas reheat device, advance back prewashing column 1 and do preliminary clearning and cooling.Flue gas after the pre-wash enters SO together with pre-wash liquid
2Demister 3 and flue gas reheat device 4 are passed through in absorption tower 2 desulfurization again, cause the chimney emptying.Make the magnesia powder of desulfurizing agent, earlier in magnesia slurry commanding tank 5, join slurry with circulating absorption solution, draw a small gangs of high-pressure fluid from circulating pump 12 outlet sides and tangentially enter, form and the homodromal rising eddy flow of stirrer paddle, do not make the blade below produce deposition from the slurry commanding tank bottom side; And circulate in forming in that water conservancy diversion heart awl is inside and outside by paddle, the magnesia powder that drops into enters heart awl with interior circulation, thick relatively particle remains on its particle diameter distribution and heart coning tower tray speed highly interval accordingly, particulate comparatively tiny or that become tiny for acid absorption liquid dissolving enters the circulating pump water inlet pipe with the top overflow, participates in the major cycle desulfurization; Circulation absorbs SO
2, its liquid-gas ratio＜4, the dynamic PH of absorption liquid desulfurization＜6.5, desulfurization degree 〉=95%; PH value in the desulfurization operation is regulated to be regulated and control by shunt volume or speed of agitator; Magnesia powder can compare continuous dosing by the required average magnesium sulphur of desulfurization.Absorb SO in circulation
2In the process, utilize surplus oxygen in the flue gas with once desulfurization product MgSO
3Partial oxidation, most of partial crystallization sinks.Play the precipitating thing with underflow pump 13 backlash of boosting, above near the precipitating layer, extract underflow liquid, a underflow liquid part that proposes is returned the absorption liquid circulatory pool through bypass and is continued to wash away, another part tangentially enters the bottom of temperature adjustment oxidation trough 6, carry dense through eddy flow, and make the overflow thin liquid of temperature adjustment oxidation trough return circulatory pool, make the MgSO in the underflow liquid
3Concentration reaches commercial production levels; When the underflow liquid concentration that proposes is low, can concentrate through eddy flow earlier, concentrate is introduced temperature adjustment oxidation trough 6 again, and the overflow thin liquid returns circulatory pool.The temperature adjustment oxidation trough can adopt steam directly to heat temperature adjustment, its bottom is provided with the tangential inlet of underflow liquid, the center is provided with the overflow pipe of two kinds of differing heights and links to each other with circulatory pool through valve, can to underflow liquid rise secondary carry dense, also can be to the mother liquor that returns through carrying dense again with underflow liquid mixed oxidization.The high underflow liquid that is deposited in the temperature adjustment oxidation trough 6 blasts air oxidation by oxidation fan, provides steam that the oxidation slurries are carried out temperature adjustment and insulation simultaneously, in case MgSO
4Crystallization before cooler crystallizer 8.The high concentration MgSO that oxidation generates
4Mixed liquor installs 7 after filtration and removes solid impurity; Cleaner liquid enters cooler crystallizer 8.In the crystallisation by cooling process, can cool off i.e. heat radiation cooling naturally through air earlier, regulate with water-cooled and by cooling water flow again and accelerate cooling velocity gradually, be cooled to 25 degree, crystallization forms the mm level coarse grain of epsom salt, finishes the initial gross separation with mother liquor and liquid phase impurity; Magma after the crystallization dewaters in centrifugal dehydrator 9 and finishes (comprising 2 dehydrations of surface washing) degree of depth separation of liquid phase impurity, after hot-air drier 10 low temperature dryings make industrial sulphuric acid magnesium.Introduce collecting tank 11 by the mother liquor that centrifugal dehydrator separates, major part can be returned the temperature adjustment oxidation trough, and fraction effluxes to keep the liquid phase impurity level of permission with boiler waste water, and also the seasonal variety of visual environment temperature is made flexible processing.
Claims (3)
1. technology is reclaimed in magnesia flue gas desulfurization and the oxidation of product thick slurry process, comprises the pre-wash cooling, common magnesia powder preparation desulfurizer slurry, the circulation absorption SO absorption tower in
2, demist and flue gas reheat sulfur removal technology step, and desulfurization slurry concentrates oxidation and desulfurization product reclaims technology, it is characterized in that, described desulfurization slurry concentrates oxidation and desulfurization product recovery technology is carried out as follows:
1) absorbs SO in circulation
2In the process, utilize surplus oxygen in the flue gas with once desulfurization product MgSO
3Partial oxidation, most of partial crystallization sinks;
2) play the precipitating thing with underflow pump (13) backlash of boosting, extract underflow liquid above near the precipitating layer, the underflow liquid part of proposition is returned the absorption liquid circulatory pool through bypass and is continued to wash away; Another part enters temperature adjustment oxidation trough (6), and makes the overflow of liquid level on the temperature adjustment oxidation trough return circulatory pool, makes the MgSO in the underflow liquid
3Concentration reaches commercial production levels; Described temperature adjustment oxidation trough bottom is provided with the tangential inlet of underflow liquid, and the center is provided with the last liquid level overflow pipe of two kinds of differing heights, underflow liquid is played secondary carry densely, and carries dense again to the mother liquor and the underflow liquid mixed oxidization that return;
3) air is blasted temperature adjustment oxidation trough (6), make MgSO
3Be oxidized to MgSO
4, and heat temperature adjustment and insulation, prevent MgSO
4Crystallization before crystallizer;
4) slurries after the temperature adjustment oxidation are removed solid impurity after filtration; Cleaner liquid adopts the water cooling crystallization to generate seven water MgSO of mm level
4Coarse grain; Magma is through centrifugal dehydration, and the mother liquor major part after the separation is returned the temperature adjustment oxidation trough; Fraction effluxes to keep the liquid phase impurity level of follow-up crystallization permission;
5) oven dry of the product after will dewatering, the control bake out temperature obtains magnesium sulfate monohydrate, epsom salt or anhydrous magnesium sulfate.
2, reclaim technology according to described magnesia flue gas desulfurization of claim 1 and the oxidation of product thick slurry process, it is characterized in that: heating temperature adjustment and being incubated described in the step 3) adopts on-site steam directly to heat temperature adjustment and insulation.
3, according to claim 1 or 2 described magnesia flue gas desulfurizations and product thick slurry process oxidation recovery technology, it is characterized in that: described common magnesia powder preparation desulfurizer slurry adopts the circulating absorption solution preparation, distributing a small gangs of absorption liquid from circulating pump (12) outlet side tangentially enters and washes away slurry commanding tank bottom, magnesia powder is one side input from the top, particle slurries tiny or refinement are introduced the circulating pump water inlet pipe from the opposite side overflow, are mixed into the absorption tower desulfurization with circulation fluid.
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| CNB2005100863878A CN100335154C (en) | 2005-09-09 | 2005-09-09 | Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process |
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| CNB2005100863878A CN100335154C (en) | 2005-09-09 | 2005-09-09 | Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process |
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| CN101658760B (en) * | 2009-09-17 | 2012-09-05 | 中节能六合天融环保科技有限公司 | Flue gas desulfurization technology applicable to calcium and magnesium desulfuraters |
| CN101804293A (en) * | 2010-04-06 | 2010-08-18 | 天津晓沃环保工程有限公司 | Flue gas desulfurization method of heating boiler and device thereof |
| CN102078750A (en) * | 2010-12-10 | 2011-06-01 | 清华大学 | Recovery method of magnesium oxide flue gas desulfurization product |
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| CN103387249A (en) * | 2013-07-31 | 2013-11-13 | 张卫东 | Method for producing magnesium sulfate by using sulfur paste and magnesium oxide as raw materials |
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| JP7380946B2 (en) | 2021-03-23 | 2023-11-15 | 富士電機株式会社 | Exhaust gas treatment equipment and exhaust gas treatment method |
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