CN100496672C - Wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction and system thereof - Google Patents
Wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction and system thereof Download PDFInfo
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Abstract
A wet flue gas desulfurization and demercuration process and a system thereof based on two-stage oxidizing reaction. The process does two-stage oxidizing treatment to the simple substance HgO in flue gas utilizing to ultraviolet radiation and oxidant of halogen series, transmutes the gas phase divalent ion Hg2+ therein to liquid phase divalent ion Hg2+ using the modified limestone-gesso wet desulfurization process, and then transmutes the liquid phase divalent ion Hg2+ to the stable mercuric sulfide-HgS deposition via stabilizer of liquid phase divalent ion Hg2+. The system comprises desulfurization and demercuration equipments such as an ultraviolet irradiator, an electrical precipitator, an oxidant spraying unit and a reaction absorber etc, gesso treatment equipments of desulfurization byproduct, and a treating equipment for mercuric sulfide-HgS deposition. The process and the system thereof can raise the oxidation rate of simple substance Hg in the flue gas effectively, and at the same time effectively overcome the reduction release of divalent ion Hg2+ to avoid secondary pollution and be capable of raise desulfurization and demercuration efficiency of limestone-gesso wet desulfurization system.
Description
Technical field
The present invention relates to the flue gases purification of coal fired power plant, refer to a kind of wet flue gas desulfurizing and hydrargyrum-removing technology and system thereof particularly based on two-stage oxidation reaction.
Background technology
Coal is the main body that China reaches interior quite over a long time from now on power station fuel at present, and coal dust firing also can bring serious mercury Hg and sulfur dioxide SO when essential thermal source and electric power resource are provided
2Pollute.According to statistics, the mercury that China's coal fired power plant in 2003 discharges in atmosphere is 86.8 tons, and the waste residue mercury emission is 28.94 tons, and mercury has severe toxicity, high volatile volatile, is easy to characteristics such as deposition and hysteresis are long in vivo, particularly enter the mercury of atmosphere, its pollution has global.The total sulfur dioxide of China's coal fired power plant discharging in 2005 is up to 2,549 ten thousand tons, and the acid rain zone of causing has thus brought tremendous loss for China's ecological environment and industrial and agricultural production near 40% of area.Therefore, fundamentally control coal fired power plant mercury Hg and sulfur dioxide SO
2Discharging extremely urgent.
At present, the means of coal-fired flue gas mercury removal mainly contain in demercuration before the burning, the burning three kinds of demercurations and burning back demercuration.Because the technology of demercuration is limited in one's ability to the removal of mercury in the fire coal in preceding demercuration of burning and the burning, so burning back demercuration is still topmost control approach.Mercury in the coal fired power plant flue gas is mainly with gaseous elemental mercury Hg
0, gaseous state divalent ion mercury Hg
2+With particle mercury Hg
PThese three kinds of forms exist, wherein gaseous elemental mercury Hg
0Account for 30～80% of flue gas total mercury content.Usually, simple substance mercury Hg
0Water insoluble, and volatility is extremely strong, and difficulty removes, and divalent ion mercury Hg
2+Soluble in water, more easily remove.
For the flue gas demercuration technology of burning back, people adopt the absorbent demercuration usually.The absorbent demercuration can be removed most gaseous state divalent ion mercury Hg
2+, and simple substance mercury Hg
0But be difficult to administer, even adopt the active carbon flue gas injection technology (ACI) of external widespread usage, to simple substance mercury Hg
0Removal effect also undesirable, and the active carbon consumption is too high, influences flying dust and utilizes, operating cost is also very high simultaneously.Can scientific and technical personnel are making great efforts research always directly utilize existing smoke eliminator such as desulphurization plant, by reasonable improvement, makes it to have concurrently the effect of demercuration.
For the coal-fired flue gas desulfurization technology, but lime stone-gypsum wet sulfur removal technology possesses skills maturation, desulfuration efficiency height, the absorbent source is wide and advantage such as desulfuration byproduct recycling, is the desulfur technology that present coal-burning power plant mainly adopts.Therefore, utilize existing lime stone-gypsum wet desulphurization plant, strengthen its demercuration performance, realize that the combined desulfurization demercuration is a kind of flue gases purification that has potentiality by reasonable improvement.
Studies show that: lime stone-gypsum wet desulphurization system is to the divalent ion mercury Hg in the flue gas
2+Has higher absorption efficiency, can realize desulfuration demercuration simultaneously, but adopt existing lime stone-gypsum wet desulphurization system demercuration also to have following problem: one, because of the simple substance mercury in the flue gas is insoluble in water, when the mercury in the flue gas is many when existing with simple substance mercury form, the demercuration efficient of this method is not high; Its two, absorb divalent ion mercury in the desulfurizer slurry easily by metal ion such as iron, manganese, nickel and sulfite ion reduction, and reenter flue gas, thereby reduced the efficient of the actual removal of mercury with the form of simple substance mercury; Its three, enter the possibility that still there is secondary pollution in mercury in desulfurization wastewater or the desulfurization slag.Therefore, improving the demercuration ability of lime stone-gypsum wet desulphurization system, reduce the reduction of divalent ion mercury simultaneously, and the mercury that captures is rationally handled, make it to form material stable, low toxicity, is the key problem that needs solution.
Publication number is that the Chinese invention patent ublic specification of application of CN1923337A has been introduced a kind of ozone O that utilizes
3As oxidant simultaneous oxidation sulfur dioxide SO
2, nitric oxide NO and simple substance mercury Hg
0, utilize the method for the desulfurization simultaneously of alkali liquid washing tower, denitration and demercuration then, but this method does not solve the divalent ion mercury Hg that is absorbed
2+Reduction problem in scrubbing tower, its actual demercuration efficient is not high, utilizes ozone O simultaneously
3With sulfur dioxide SO
2Be oxidized to sulfur trioxide SO
3Be unfavorable for desulfurization on the contrary, this is because sulfur trioxide SO
3In scrubbing tower, form tiny aerosol particle easily, stop to absorb slurries and sulfur trioxide SO
3Further reaction.Publication number is the method that the Chinese invention patent ublic specification of application of CN1895745A has proposed a kind of mercury removal for smoke desulfurizing system by fortified wetting, and this method is by spraying into halogenic molecule or its compound with simple substance mercury Hg in flue
0Be oxidized to divalent ion mercury Hg
2+, again flue gas is imported wet desulfurization system, and in desulfurizer slurry, add liquid phase mercury stabilizing agent, reach the purpose of demercuration.But this method does not solve divalent ion mercury Hg in the absorption tower equally
2+Reduction discharge problem.In addition, this method is to simple substance mercury Hg
0Carry out stair oxidation and handle,, must spray into excessive oxidant, and excessive oxidant will inevitably cause secondary pollution if will realize higher mercury oxidation rate.Publication number is that the Chinese invention patent ublic specification of application of CN1933894A discloses a kind of method that bromine-containing compound strengthens the oxidation of mercury that adds from coal or in the boiler-burner, this method improves the content of divalent ion mercury in the flue gas by the oxidation of bromo element, in the hope of improving the removal of mercury ability of wet type desulfurizing system, but it is very limited to the oxidability of simple substance mercury to add bromine-containing compound in combustion process, thereby has limited the removal of mercury ability of wet type desulfurizing system.
Summary of the invention
Purpose of the present invention is exactly that a kind of wet flue gas desulfurizing and hydrargyrum-removing technology and system thereof based on two-stage oxidation reaction will be provided.Adopt this technology and system thereof can effectively improve the oxygenation efficiency of simple substance mercury in the flue gas, the reduction that can effectively overcome the divalent ion mercury that generates simultaneously discharges problem, can also significantly improve the desulfuration demercuration efficient of lime stone-gypsum wet desulphurization system.
For achieving the above object, the present invention organically combines a plurality of processing steps and is one to act synergistically mutually, realizes primary oxidation, the deep oxidation of mercury in the flue gas by different level, and desulfuration demercuration and divalent ion mercury are fixed.The designed wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction adopts ultraviolet ray and halogen oxidant to the simple substance mercury Hg in the flue gas
0Carry out two-stage oxidation and handle, and make wherein gas phase divalent ion mercury Hg by improved lime stone-gypsum wet sulfur removal technology
2+Be converted into liquid phase divalent ion mercury Hg
2+, and then by liquid phase divalent ion mercury Hg
2+Stabilizing agent makes liquid phase divalent ion mercury Hg
2+Be converted into stable mercuric sulphide HgS precipitation.Its specific embodiment comprises the steps:
1) adopt the photocatalyst of ultraviolet ray as primary oxidation, the flue gas with its irradiation coal-burning boiler unit is given off makes most simple substance mercury Hg in the flue gas
0With sulfur dioxide, oxygen sufficient oxidation reaction taking place, generates solid phase mercury compound mereurous sulfate and mercury oxide;
2) to carrying out the electrostatic precipitation processing through the ultraviolet flue gas that shines, remove in the flue gas grit that is contained and solid phase mercury compound mereurous sulfate and the mercury oxide that is generated;
3) adopt halogen simple substance or its compound as the deep oxidation agent, it is ejected in the flue gas of handling through electrostatic precipitation, make simple substance mercury Hg remaining in the flue gas
0With halogen simple substance or its compound sufficient oxidation reaction taking place, generates the gas phase divalent ion mercury Hg that is easy to remove
2+
4) will import lime stone-gypsum wet desulphurization system through the flue gas of deep oxidation, make sulfur in smoke and gas phase divalent ion mercury Hg
2+React with the calcium-base absorbing agent slurries respectively, generate calcium sulfite and liquid phase divalent ion mercury Hg
2+, in the calcium-base absorbing agent slurries, add liquid phase divalent ion mercury Hg simultaneously
2+Stabilizing agent makes liquid phase divalent ion mercury Hg
2+Be converted into stable mercuric sulphide HgS precipitation, prevent liquid phase divalent ion mercury Hg
2+Reduction is released into simple substance mercury Hg
0
5) the calcium-base absorbing agent slurries through the desulfuration demercuration reaction are carried out forced oxidation, make calcium sulfite wherein change into calcium sulfate,, obtain by-produced gypsum, and discharge desulfurization wastewater again by rotational flow separation and processed;
6) flue gas through the desulfuration demercuration reaction is carried out demist and handle, remove drop entrained in the flue gas, isolate clean flue gas simultaneously.
Above-mentioned steps 1) in, preferentially adopting wavelength is that the ultraviolet irradiation temperature of 220～280nm is 536～662 ℃ a flue gas.Be fit under the temperature and wavelength condition of reaction at this, ultraviolet ray photocatalyst can impel the simple substance mercury Hg more than 80%
0React with sulfur dioxide and oxygen, generate solid phase mercury compound mereurous sulfate and mercury oxide, thereby realize simple substance mercury Hg
0Primary oxidation.The equation of its chemical reaction is as follows:
2Hg+O
2+SO
2＝(Hg)
2SO
4
2Hg+O
2＝2HgO
Above-mentioned steps 2) in, disposed by electrostatic precipitator, can significantly reduce the consumption of oxidant in the follow-up hydrargyrum-removing technology, thereby subsequent technique is oversimplified through most solid phase mercury compound mereurous sulfates and mercury oxide that the ultraviolet catalyzed reaction is generated.
Above-mentioned steps 3) in, preferentially adopts chlorine Cl
2Or its compound is as the deep oxidation agent, and it is ejected into temperature is in 110～130 ℃ the flue gas, remaining simple substance mercury Hg in its emitted dose and the flue gas
0Stoichiometric proportion be 10～10
3: 1.Can certainly adopt other kin halogen simple substance such as bromine gas Br
2Or its compound is as the deep oxidation agent.Under this preferred temperature and metering proportion, help chlorine Cl more
2With simple substance mercury Hg
0Oxidation reaction.Its reaction equation is as follows:
Hg+Cl
2＝HgCl
2
Meanwhile, the fly ash granule in the flue gas also can promote simple substance mercury Hg
0Oxidation, only need spray into a spot of chlorine Cl thus
2Just can be to simple substance mercury Hg remaining in the flue gas
0Carry out deep oxidation, realize simple substance mercury Hg
0To divalent ion mercury Hg
2+Conversion fully.Simultaneously, Xiao Jiliang chlorine Cl
2Also alleviated its corrosiveness, be convenient to solve the defective workmanship that excessive oxidant brings flue.
Above-mentioned steps 4) in, sulfur dioxide SO
2As follows with the equation of calcium-base absorbing agent slurries generation chemical reaction:
CaCO
3+SO
2+(1/2)H
2O＝CaSO
3●(1/2)H
2O+CO
2
Gas phase divalent ion mercury Hg
2+As follows with the equation of calcium-base absorbing agent slurries generation chemical reaction:
HgCl
2+CaCO
3＝HgCO
3+CaCl
2
Excessive oxidant chlorine Cl
2Also, generate calcium chloride with calcium-base absorbing agent slurries generation chemical reaction.Like this, in flue gas desulfurization, also with the gas phase divalent ion mercury Hg in the flue gas
2+Conversion is for liquid phase divalent ion mercury Hg
2+
Above-mentioned steps 4) in, liquid phase divalent ion mercury Hg
2+Stabilizing agent preferentially adopts NaHS NaHS.NaHS NaHS can effectively suppress liquid phase divalent ion mercury Hg
2+Discharged by metal ion such as iron, manganese, nickel, cobalt and sulfite ion reduction:
With Me
2+Represent above-mentioned metal ion, itself and liquid phase divalent ion mercury Hg
2+Reaction equation as follows:
2Me
2++Hg
2+＝Hg
0+2Me
3+
Sulfite ion and liquid phase divalent ion mercury Hg
2+Reaction equation as follows:
HSO
3 -+H
2O+Hg
2+＝Hg
0+SO
4 2-+3H
+
And after having added NaHS NaHS, its reaction equation is as follows:
NaHS＝Na
++H
++S
2-
Hg
2++S
2-＝HgS
Mercuric sulphide HgS is stable precipitation, by adding NaHS NaHS, can effectively suppress ionic liquid phase mercury Hg like this
2+Reduction discharge.
Above-mentioned steps 5) in, the reaction equation of the calcium-base absorbing agent slurries through the desulfuration demercuration reaction being carried out the forced oxidation processing is as follows:
CaSO
3·(1/2)H
2O+(1/2)O
2+(3/2)H
2O＝CaSO
4·2H
2O
Thus the calcium sulfite in the calcium-base absorbing agent slurries is changed into calcium sulfate, gained calcium sulfate can pass through rotational flow separation, processed, acquisition by-produced gypsum.
Above-mentioned steps 5) in, in the desulfurization wastewater of discharging, adds flocculation aid and liquid phase divalent ion mercury Hg
2+Stabilizing agent, flocculation aid preferentially adopt policapram, liquid phase divalent ion mercury Hg
2+Stabilizing agent preferentially adopts vulcanized sodium Na
2S or organic sulfur, its reaction equation is as follows:
Hg
2++S
2-＝HgS
Thus can be with liquid phase divalent ion mercury Hg residual in the desulfurization wastewater
2+Be converted into stable mercuric sulphide HgS precipitation fully, thereby effectively suppress the secondary pollution of mercury.
For realizing the custom-designed wet flue gas desulfurizing and hydrargyrum-removing system of above-mentioned technology based on two-stage oxidation reaction, mainly by the electrostatic precipitator that is used for the pre-dust removal process of flue gas, be used for the reaction absorption tower that flue gas desulfurizing and hydrargyrum-removing handles and gypsum cyclone, gypsum dehydration device and the desulfurization wastewater cyclone etc. that constitute the desulfurizing byproduct treatment system are formed.Flue before the described electrostatic precipitator import is provided with ultraviolet radiation device, and the flue after the described electrostatic precipitator outlet is provided with oxidizer injection device, and the exhaust pass of described oxidizer injection device links to each other with the import on reaction absorption tower.Described reaction absorption tower is provided with stock tank district, bottom from bottom to top successively, flue gas input area, bottom, absorbent spray district, middle part, and flue gas demist district, top, wherein: the stock tank district, bottom on reaction absorption tower is connected with lime stone slurry device for supplying and air apparatus for feeding, the flue gas input area, bottom on reaction absorption tower is provided with gas approach, the absorbent spray district, middle part on reaction absorption tower is furnished with the lime stone slurry spraying layer, the flue gas demist district, top on reaction absorption tower is furnished with demister, links to each other by external slurry circulating pump between stock tank district, bottom and the lime stone slurry spraying layer on reaction absorption tower.
Further, the underflow head piece of described desulfurization wastewater cyclone links to each other with the waste water Buffer Pool, and described waste water Buffer Pool links to each other with ionic liquid phase mercury reaction chamber by infusion pump, and described ionic liquid phase mercury reaction chamber communicates with depositing reservoir.In ionic liquid phase mercury reaction chamber, residual liquid phase divalent ion mercury Hg in the desulfuration demercuration waste water
2+Can be converted into mercuric sulphide HgS precipitation fully, by gravitational settling, mercuric sulphide HgS precipitation is separated from desulfuration demercuration waste water again, obtained the demercuration byproduct, discharge the desulfuration demercuration waste water of allow compliance with emission standards simultaneously, realize the innoxious and recycling of desulfuration demercuration product.
Compared with prior art, the present invention has following advantage:
One, the present invention organically is combined into a complete process system with flue gas desulfurizing and hydrargyrum-removing technology and device, has both simplified technological process, has simplified system architecture, has reduced occupation area of equipment, has significantly reduced the investment and the operating cost of equipment again.
Its two, the present invention adopts two-stage flue gas oxidation technology, the ultraviolet ray that is used for primary oxidation is with about 80% simple substance mercury Hg
0Be oxidized to divalent ion mercury Hg
2+, so significantly reduced the amount of the required halogen oxidant of deep oxidation, avoided introducing excess halogen class oxidant and the difficult problem that causes boiler flue corrosion, also effectively controlled owing to the excessive secondary pollution that causes of halogen oxidant.The two-stage oxidation program can be guaranteed the simple substance mercury Hg in the flue gas simultaneously
0Change into divalent ion mercury Hg fully
2+, and then significantly improve the removal of mercury efficient of desulphurization system.
Its three, the present invention is by injecting liquid phase divalent ion mercury Hg in the calcium-base absorbing agent slurries of lime stone-gypsum wet sulfur removal technology
2+Stabilizing agent has effectively suppressed liquid phase divalent ion mercury Hg
2+Reduction discharge, simultaneously the mercury that captures is converted into the stable compound mercuric sulphide HgS of low toxicity, both greatly improved the demercuration efficient of whole system, suppress the secondary pollution of mercury again effectively.
Its three, desulfuration demercuration byproduct of the present invention is gypsum and mercuric sulphide, can realize the innoxious and recycling of desulfuration demercuration accessory substance.
In sum, the present invention has little, the characteristics such as energy consumption is low, process system is simple, operating cost is low, absorbent utilization rate height, operational reliability height of investment, it can not only effectively suppress the primary pollution and the secondary pollution of mercury and oxidant, and can significantly improve the desulfuration demercuration efficient of lime stone-gypsum wet sulfur removal technology, its desulfuration efficiency can reach more than 95%, demercuration efficient can reach more than 90%, and treated flue gas meets the national standard of coal-fired flue-gas pollutant emission fully.
Description of drawings
Accompanying drawing is a kind of structural representation of the wet flue gas desulfurizing and hydrargyrum-removing system based on two-stage oxidation reaction.
The specific embodiment
Below at a coal-burning boiler unit, the present invention is described in further detail in conjunction with the accompanying drawings:
The wet flue gas desulfurizing and hydrargyrum-removing system based on two-stage oxidation reaction shown in the figure is by equipment such as ultraviolet radiation device 3, electrostatic precipitator 5 and oxidizer injection devices 6 and be connected the two-stage flue gas oxidative system that flue constitutes; By equipment such as flue gas heat exchange device 7, reaction absorption tower 8, air-introduced machine 9 and chimney 10 and be connected the flue gas desulfurizing and hydrargyrum-removing system that flue constitutes; Constitute desulfurizing byproduct gypsum treatment system by equipment such as gypsum cyclone 14, gypsum dehydration device 13 and desulfurization wastewater cyclone 11 and connecting line thereof; Constitute mercuric sulphide HgS precipitation process system by equipment such as waste water Buffer Pool 19, ionic liquid phase mercury reaction chamber 20, depositing reservoir 21 and connecting line thereof.
It is the 253.7nm ultraviolet emission device that ultraviolet radiation device 3 adopts wavelength, be arranged on the economizer 2 and the flue between the air preheater 4 of coal-burning boiler unit 1, the flue-gas temperature at this place is than being easier to be controlled in 536～662 ℃ the scope, and this also is simple substance mercury Hg
0Optimum temperature range with sulfur dioxide and oxygen generation oxidation reaction.The outlet of air preheater 4 links to each other with the import of electrostatic precipitator 5, the outlet of electrostatic precipitator 5 links to each other with the import of oxidizer injection device 6, oxidizer injection device 6 adopts the spray nozzle that has barrier, can some female pipes and arm specifically be set according to the flue cross-sectional sizes, and the quantity of atomizer on the arm, the outlet of oxidizer injection device 6 links to each other by the import of flue gas heat exchange device 7 with reaction absorption tower 8.Serve as a contrast anti-corrosion material on the flue inwall between oxidizer injection device 6 and the reaction absorption tower 8.
Reaction absorption tower 8 is a tubular construction, is provided with stock tank district, bottom, flue gas input area, bottom, middle part absorbent spray district and flue gas demist district, top from bottom to top successively.Wherein: the stock tank district, bottom on reaction absorption tower 8 is connected with lime stone slurry device for supplying 17 and air apparatus for feeding 18.The flue gas input area, bottom on reaction absorption tower 8 is provided with gas approach.The absorbent spray district, middle part on reaction absorption tower 8 is furnished with lime stone slurry spraying layer 82.The flue gas demist district, top on reaction absorption tower 8 is furnished with demister 83, demister 83 adopts the combination demister, constitute by upper and lower layer demist filter screen and the cleaning sprinkler part between upper and lower layer demist filter screen, can completely effectively the moisture content that is contained in the flue gas be separated.The top exhanst gas outlet on reaction absorption tower 8 links to each other with chimney 10 by flue gas heat exchange device 7, air-introduced machine 9, link to each other by external slurry circulating pump 16 between stock tank district, bottom and the lime stone slurry spraying layer 82 on reaction absorption tower 8, uninterruptedly circulate to guarantee the lime stone absorbent slurry.
In order to improve the reaction condition of reaction absorption tower 8 interior flue gases and lime stone slurry, below lime stone slurry spraying layer 82, also be provided with flue gas uniform device 81, flue gas uniform device 81 is the hypocrateriform structure, is evenly distributed with many through holes that lime stone slurry is detained and passes of being convenient on its card.Design like this, when flue gas upwards passed through the porous pallet, can make distributes on the cross section of flue gas in reaction absorption tower 8 was tending towards evenly, thereby strengthens sulfur in smoke and gas phase divalent ion mercury Hg on the one hand
2+With the contact-making surface of lime stone slurry, improve the reaction rate of lime stone slurry and flue gas greatly; The lime stone slurry of ejection upwards from lime stone slurry spraying layer 82 on the other hand, when falling after rise to the porous pallet, form certain thickness slurry layer thereon, this slurry layer is worn under the effect of penetrating the flue gas stream that makes progress, produce violent bubbling phenomenon, but time of contact of prolong smoke and lime stone slurry is not only improved the desulfuration demercuration efficient of whole device, and can effectively remove a part of flying dust, and then improve the efficiency of dust collection of whole system.Distance design between lime stone slurry spraying layer 82 and the flue gas uniform device 81 is between 0.8～1.5m, and this spacing need not increase any auxiliary stand just can carry out conventional installing/dismounting and maintenance to lime stone slurry spraying layer 82 easily.
The plasma discharge mouth of reaction 8 bottoms, absorption tower links to each other with the import of gypsum cyclone 14 by slurry pump 15, and the underflow head piece of gypsum cyclone 14 links to each other with gypsum dehydration device 13; The last overfall of gypsum cyclone 14 links to each other with desulfurization wastewater cyclone 11.The underflow head piece of desulfurization wastewater cyclone 11 links to each other with waste water Buffer Pool 19, and waste water Buffer Pool 19 links to each other with ionic liquid phase mercury reaction chamber 21 by infusion pump 20, and ionic liquid phase mercury reaction chamber 21 communicates with depositing reservoir 22; The last overfall of desulfurization wastewater cyclone 11 links to each other with filtrate box 12.
Wet flue gas desulfurizing and hydrargyrum-removing technology process based on two-stage oxidation reaction of the present invention is such:
At first, the high-temperature flue gas of producing from coal-burning boiler unit 1 enters into ultraviolet radiation device 3 by economizer 2, the temperature of control flue gas is in 536～662 ℃ scope, ultraviolet radiation device 3 is launched the ultraviolet ray that wavelength is 253.7nm, the uniform irradiation flue gas makes the simple substance mercury Hg more than 80% in the flue gas
0With sulfur dioxide and oxygen sufficient oxidation reaction taking place, generate solid phase mercury compound mereurous sulfate and mercury oxide, realizes the primary oxidation of flue gas.
Secondly, entered into electrostatic precipitator 5 by the flue gas of primary oxidation by air preheater 4, most of dust that is contained in the flue gas and particulate form solid phase mercury compound are removed by electrostatic precipitator 5.
Once more, flue gas flows out from the outlet of electrostatic precipitator 5, enters into oxidizer injection device 6, and the temperature of control flue gas is in 110～130 ℃ scope, and oxidizer injection device 6 sprays into an amount of chlorine Cl to flue gas
2, remaining simple substance mercury Hg in its emitted dose and the flue gas
0Stoichiometric proportion be 100:1, make simple substance mercury Hg remaining in the flue gas
0With chlorine Cl
2Sufficient oxidation reaction takes place, and generates the gas phase divalent ion mercury Hg that is easy to remove
2+, the deep oxidation of realization flue gas.By above-mentioned two-stage oxidation, can make the simple substance mercury Hg in the flue gas
0Be converted into gas phase divalent ion mercury Hg fully
2+
Then, the flue gas of process two-stage oxidation enters into reaction absorption tower 8 by flue gas heat exchange device 7, with reverse contact of lime stone slurry from 82 ejections of lime stone slurry spraying layer, fierce gas-liquid two-phase takes place react, and makes sulfur in smoke SO
2Change into calcium sulfite, simultaneously with the gas phase divalent ion mercury Hg in the flue gas
2+Change into liquid phase divalent ion mercury Hg
2+Excessive chlorine Cl in the flue gas
2Also can with the lime stone slurry generation calcium chloride that reacts.Meanwhile, in lime stone slurry device for supplying 17, add liquid phase divalent ion mercury Hg
2+Stabilizing agent, liquid phase divalent ion mercury Hg
2+Stabilizing agent adopts NaHS NaHS, makes liquid phase divalent ion mercury Hg
2+Be converted into stable mercuric sulphide HgS precipitation, prevent liquid phase divalent ion mercury Hg
2+Reduction is released into simple substance mercury Hg
0
Again, the oxygen forced oxidation that the lime stone slurry that reacts through desulfuration demercuration is ejected by air apparatus for feeding 18, calcium sulfite wherein changes into calcium sulfate, the slurries of sulfur acid calcium are from the plasma discharge mouth output of reaction 8 bottoms, absorption tower, deliver to gypsum cyclone 14 by slurry pump 15, the underflow stream of gypsum cyclone 14 enters into gypsum dehydration device 13 and handles, and finally obtains the desulfuration demercuration by-produced gypsum.The overflow stream of gypsum cyclone 14 enters into desulfurization wastewater cyclone 11 eddy flow once more, and the last overflow of desulfurization wastewater cyclone 11 is sent in the filtrate box 12, and it is recycling to send reaction absorption tower 8 after filtering back to.The underflow stream of desulfurization wastewater cyclone 11 then enters in the waste water Buffer Pool 19, and the waste water in the waste water Buffer Pool 19 is delivered to ionic liquid phase mercury reaction chamber 21 by infusion pump 20 again.In ionic liquid phase mercury reaction chamber 21, be added with flocculation aid and liquid phase divalent ion mercury Hg
2+Stabilizing agent, flocculation aid adopts policapram, liquid phase divalent ion mercury Hg
2+Stabilizing agent then adopts vulcanized sodium Na
2S or organic sulfur, residual liquid phase divalent ion mercury Hg in the waste water
2+Can be converted into the mercuric sulphide HgS precipitation of stablizing low toxicity fully at this.The waste water of discharging from ionic liquid phase mercury reaction chamber 21 flows to depositing reservoir 22, utilizes the gravitational settling effect to obtain demercuration byproduct mercuric sulphide HgS, and the desulfuration demercuration technique waste water that reaches discharge standard is discharged by depositing reservoir 22 top gaps.
At last, the flue gas of handling through desulfuration demercuration enters in the demister 83 on reaction 8 tops, absorption tower, removes drop entrained in the flue gas, and isolated clean flue gas is discharged by the top exhanst gas outlet, through flue gas heat exchange device 7 temperature is raised to about 80 ℃, pumps to chimney 10 by air-introduced machine 9 again.
Claims (10)
1, a kind of wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction comprises the steps:
1) adopt the photocatalyst of ultraviolet ray as primary oxidation, the flue gas with its irradiation coal-burning boiler unit is given off makes most simple substance mercury Hg in the flue gas
0With sulfur dioxide and oxygen sufficient oxidation reaction taking place, generates solid phase mercury compound mereurous sulfate and mercury oxide;
2) to carrying out the electrostatic precipitation processing through the ultraviolet flue gas that shines, remove in the flue gas grit that is contained and the solid phase mercury compound that is generated;
3) adopt halogen simple substance as the deep oxidation agent, it is ejected in the flue gas of handling through electrostatic precipitation, make simple substance mercury Hg remaining in the flue gas
0With halogen simple substance sufficient oxidation reaction taking place, generates the gas phase divalent ion mercury Hg that is easy to remove
2+
4) will import lime stone-gypsum wet desulphurization system through the flue gas of deep oxidation, make sulfur in smoke and gas phase divalent ion mercury Hg
2+React with lime stone slurry respectively, generate calcium sulfite and liquid phase divalent ion mercury Hg
2+, in lime stone slurry, add liquid phase divalent ion mercury Hg simultaneously
2+Stabilizing agent makes liquid phase divalent ion mercury Hg
2+Be converted into stable mercuric sulphide HgS precipitation, prevent liquid phase divalent ion mercury Hg
2+Reduction is released into simple substance mercury Hg
0
5) lime stone slurry through the desulfuration demercuration reaction is carried out forced oxidation, make calcium sulfite wherein change into calcium sulfate,, obtain by-produced gypsum, and discharge desulfurization wastewater again by rotational flow separation and processed;
6) flue gas through the desulfuration demercuration reaction is carried out demist and handle, remove drop entrained in the flue gas, isolate clean flue gas simultaneously.
2, the wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction according to claim 1 is characterized in that: in the said step 1), the employing wavelength is that the ultraviolet irradiation temperature of 220～280nm is 536～662 ℃ a flue gas.
3, the wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction according to claim 1 is characterized in that: in the said step 3), adopt chlorine Cl
2As the deep oxidation agent, it is ejected into temperature is in 110～130 ℃ the flue gas, remaining simple substance mercury Hg in its emitted dose and the flue gas
0Stoichiometric proportion be 10～10
3: 1.
4, the wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction according to claim 1 is characterized in that: in the said step 4), and liquid phase divalent ion mercury Hg
2+Stabilizing agent adopts NaHS NaHS.
5, the wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction according to claim 1 is characterized in that: in the said step 5), add flocculation aid and liquid phase divalent ion mercury Hg in the desulfurization wastewater of discharging
2+Stabilizing agent makes liquid phase divalent ion mercury Hg residual in the desulfurization wastewater
2+Be converted into stable mercuric sulphide HgS precipitation fully.
6, the wet flue gas desulfurizing and hydrargyrum-removing technology based on two-stage oxidation reaction according to claim 5 is characterized in that: said flocculation aid adopts policapram, liquid phase divalent ion mercury Hg
2+Stabilizing agent adopts vulcanized sodium Na
2S or organic sulfur.
7, a kind ofly adopt the described technology of claim 1 and custom-designed wet flue gas desulfurizing and hydrargyrum-removing equipment based on two-stage oxidation reaction, comprise gypsum cyclone (14), gypsum dehydration device (13) and the desulfurization wastewater cyclone (11) of the electrostatic precipitator (5) that is used for the pre-dust removal process of flue gas, the reaction absorption tower (8) that is used for the flue gas desulfurizing and hydrargyrum-removing processing and formation desulfurizing byproduct treatment facility, it is characterized in that:
Flue before described electrostatic precipitator (5) import is provided with ultraviolet radiation device (3), flue after described electrostatic precipitator (5) outlet is provided with oxidizer injection device (6), and the exhaust pass of described oxidizer injection device (6) links to each other with the import on reaction absorption tower (8);
Described reaction absorption tower (8) is provided with stock tank district, bottom from bottom to top successively, flue gas input area, bottom, absorbent spray district, middle part, and flue gas demist district, top, wherein: the stock tank district, bottom on reaction absorption tower (8) is connected with lime stone slurry device for supplying (17) and air apparatus for feeding (18), the flue gas input area, bottom on reaction absorption tower (8) is provided with gas approach, the absorbent spray district, middle part on reaction absorption tower (8) is furnished with lime stone slurry spraying layer (82), the flue gas demist district, top on reaction absorption tower (8) is furnished with demister (83), links to each other by external slurry circulating pump (16) between stock tank district, bottom and the lime stone slurry spraying layer (82) on reaction absorption tower (8).
8, the wet flue gas desulfurizing and hydrargyrum-removing equipment based on two-stage oxidation reaction according to claim 7, it is characterized in that: the underflow head piece of described desulfurization wastewater cyclone (11) links to each other with waste water Buffer Pool (19), described waste water Buffer Pool (19) links to each other with ionic liquid phase mercury reaction chamber (21) by infusion pump (20), and described ionic liquid phase mercury reaction chamber (21) communicates with depositing reservoir (22).
9, according to claim 7 or 8 described wet flue gas desulfurizing and hydrargyrum-removing equipment based on two-stage oxidation reaction, it is characterized in that: described ultraviolet radiation device (3) is arranged on the economizer (2) and the flue between the air preheater (4) of coal-burning boiler unit (1).
10, according to claim 7 or 8 described wet flue gas desulfurizing and hydrargyrum-removing equipment based on two-stage oxidation reaction, it is characterized in that: lime stone slurry spraying layer (82) below in the described reaction absorption tower (8) is provided with flue gas uniform device (81), described flue gas uniform device (81) is the hypocrateriform structure, is evenly distributed with many through holes that lime stone slurry is detained and passes of being convenient on its card.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9457316B2 (en) * | 2012-07-12 | 2016-10-04 | The Babcock & Wilcox Company | Method for controlling compounds and conditions in a wet flue gas desulfurization (WFGD) unit |
| US10018356B2 (en) | 2012-07-12 | 2018-07-10 | The Babcock & Wilcox Company | System and method for controlling one or more process parameters associated with a combustion process |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4893617B2 (en) * | 2007-12-27 | 2012-03-07 | 株式会社Ｉｈｉ | Mercury removal apparatus and mercury removal method |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1562445A (en) * | 2004-03-29 | 2005-01-12 | 广东杰特科技发展有限公司 | Method of synchronous cleansing air pollutant by smoke of plasma discharge caused by spreading light |
| EP1524023A1 (en) * | 2003-10-17 | 2005-04-20 | The Boc Group, Inc. | Improved process for the removal of contaminants from gas streams |
| CN1864813A (en) * | 2006-04-20 | 2006-11-22 | 上海交通大学 | Method for simultaneous purification of elementary substance mercury and nitric oxides in coal-fired flue gas |
| CN1883768A (en) * | 2006-05-29 | 2006-12-27 | 浙江大学 | Wet method combined process for desulfurization and denitration for chlorine-containing strong oxidizer absorption liquid |
| CN1895745A (en) * | 2006-06-29 | 2007-01-17 | 上海交通大学 | Mercury removal for smoke desulfurizing system by fortified wetting method |
| CN1923337A (en) * | 2006-08-23 | 2007-03-07 | 浙江大学 | Boiler smoke gas multipollutant ozonization and simultaneous elimination device and method therefor |
-
2007
- 2007-04-30 CN CNB2007100521282A patent/CN100496672C/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1524023A1 (en) * | 2003-10-17 | 2005-04-20 | The Boc Group, Inc. | Improved process for the removal of contaminants from gas streams |
| CN1562445A (en) * | 2004-03-29 | 2005-01-12 | 广东杰特科技发展有限公司 | Method of synchronous cleansing air pollutant by smoke of plasma discharge caused by spreading light |
| CN1864813A (en) * | 2006-04-20 | 2006-11-22 | 上海交通大学 | Method for simultaneous purification of elementary substance mercury and nitric oxides in coal-fired flue gas |
| CN1883768A (en) * | 2006-05-29 | 2006-12-27 | 浙江大学 | Wet method combined process for desulfurization and denitration for chlorine-containing strong oxidizer absorption liquid |
| CN1895745A (en) * | 2006-06-29 | 2007-01-17 | 上海交通大学 | Mercury removal for smoke desulfurizing system by fortified wetting method |
| CN1923337A (en) * | 2006-08-23 | 2007-03-07 | 浙江大学 | Boiler smoke gas multipollutant ozonization and simultaneous elimination device and method therefor |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9457316B2 (en) * | 2012-07-12 | 2016-10-04 | The Babcock & Wilcox Company | Method for controlling compounds and conditions in a wet flue gas desulfurization (WFGD) unit |
| US10018356B2 (en) | 2012-07-12 | 2018-07-10 | The Babcock & Wilcox Company | System and method for controlling one or more process parameters associated with a combustion process |
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|---|---|
| CN101053738A (en) | 2007-10-17 |
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