CN201195095Y - Waste gas purifier - Google Patents
Waste gas purifier Download PDFInfo
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- CN201195095Y CN201195095Y CNU2008200589482U CN200820058948U CN201195095Y CN 201195095 Y CN201195095 Y CN 201195095Y CN U2008200589482 U CNU2008200589482 U CN U2008200589482U CN 200820058948 U CN200820058948 U CN 200820058948U CN 201195095 Y CN201195095 Y CN 201195095Y
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- absorption liquid
- waste gas
- washing
- purification apparatus
- gas purification
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Abstract
The utility model relates to a purifying train for exhaust gas, in particular to a purifying and treating device for acid pollutant in the exhaust gas. The purifying and treating device comprises purifying equipment with special structure. A washing absorption section is arranged at the higher position inside the purifying equipment, and the washing absorption section comprises an absorption-liquid distributor; an absorption-liquid storing section is arranged at the lower position inside the purifying equipment. The exhaust gas enters the washing absorption section from a raw exhaust gas inlet positioned at a higher position, and the solid granule rejectamenta and harmful gases, especially the acid exhaust gases are absorbed by the washing absorption section, meanwhile, the absorption liquid enters the absorption liquid storing section which is arranged at the lower position and realizes liquid circulation with the washing absorption section, at the same time, functions of oxidation, separating out, crystal formation, separation, and the like are integrated, so the working efficiency of the purifying equipment can be markedly improved. The utility model has the advantages of little investment, little energy consumption, great exhaust gas treating ability and high efficiency, and is suitable for large-scale industrial application.
Description
Technical field
The utility model relates to the purifier of waste gas, relates in particular to acid contaminant in the waste gas, comprises deviating from and purifying processing device of oxysulfide, applicable to technical fields such as electric power, metallurgy, chemical industry and environmental protection.
Background technology
With coal or oil is the boiler or the thermal power plant of fuel, perhaps is that a large amount of flue gases are discharged by raw material sintering smeltery with the iron ore.These waste gas contain harmful gaseous substances such as SOx, NOx, HCl and HF, and salic, silica, the fine coal dust of solids such as iron oxide.Its sulphur oxide SOx comprises SO
2And SO
3, be the main matter that forms acid rain.
SO
2Content is usually at 300～5000ppmv (1000～15000mg/Nm
3) between, dust content 100-300mg/Nm
3Between.But exhausted air quantity is very huge, and the opinion with coal-burning boiler, steam scale are from 35T/h to 2500T/h, and generating set capacity 6MW is to 1000MW, and exhausted air quantity is by 50,000 Nm
3/ h to 250 ten thousand Nm
3, SO
21000 tons/year to 100,000 tons/year of discharge capacitys.Because SOx is a sour gas, adopt alkaline aqueous solution to take off the SOx that inhales in the waste gas, i.e. (Flue GasDesulfurization FGD) is effective method, is with a wide range of applications in waste gas sulphur removal.
The method of waste gas sulphur removal is more, according to the difference of the raw material that is adopted, mainly contains following several method:
With the lime stone is the calcium method of raw material;
With ammonia is the ammonia process of raw material;
With magnesia is the magnesium method of raw material;
Industrial, prior art mainly is the calcium method.Because lime stone solubility in water is very low, has only 30-50mg/L, must grind into superfines, and generally based on wet-milling, the fineness of lime stone reaches greater than 325 purpose ratios greater than 90%.The reaction principle of calcium method is as follows.
SO
2+H
2O＝H
2SO
3
H
2SO
3+ CaCO
3(lime stone)=CaSO
3.1/2H
2O ↓+CO
2↑+H
2O
CaSO
3.1/2H
2O+1/2O
2+ 3/2H
2O=CaSO
4.2H
2O ↓ (gypsum)
Waste gas at first contacts with the pulpous state absorption liquid that contains ultra-fine lime stone, SO wherein
2Be dissolved in the aqueous solution, form sulfurous acid, again with absorption liquid in calcium carbonate reaction, form calcium sulfite hemihydrate, emit carbon dioxide simultaneously.Calcium sulfite hemihydrate and the calcium carbonate solubility in water is close.In order to improve the solubility of calcium, reduce the obstruction of equipment, adopt the way of drum air oxidation, the inferior calcium sulfite hemihydrate that solubility is low excessively is converted into the higher calcium sulfate of solubility.Under similarity condition, the solubility of calcium sulfate is 30 times.Simultaneously, calcium sulfate precipitation is a gypsum, i.e. calcium sulphate dihydrate has than calcium sulfite hemihydrate purposes more greatly, can be used as construction material, especially as the additive of cement.This also is the reason why present industrialized waste gas sulphur removal calcium method all needs the drum air oxidation.
The calcium method has application promise in clinical practice in China, and China has abundant natural limestone mineral resources.In addition, China has huge building materials market, especially cement industry.Therefore, calcium method waste gas sulphur removal process can obtain extensive use in China.But, because China also has very huge plaster of paris resource, and also very huge by the ardealite output of huge phosphate fertilizer industrial by-product, also limited applying of calcium method waste gas sulfur removal technology to a great extent.
In addition, because the boiler of power plant waste gas dedusting efficient of China also is not very high at present, the product quality of sulphur removal gypsum is relatively poor, has also directly influenced its application.
For this reason, need seek other method.
The ammonia process that with ammonia is raw material comprises three concrete steps:
(1) SO
2Absorb:
SO
2+2NH
3+H
2O＝(NH
4)
2SO
3
(2) ammonium sulfurous oxidation
SO
3 2-+1/2O
2＝SO
4 2-
(3) sulphur crystalline ammonium:
(NH
4)
2SO
4(L)＝(NH
4)
2SO
4(S)
Therefore, ammonia process sulphur removal process is produced ammonium sulfate, a kind of high-effective chemical fertilizer, and its fertilizer efficiency doubles than carbon ammonium, than urea also high 20%.Available nitrogen N in the raw material ammonia is worth at 18～19 yuan/N, and still, in the sulphur ammonium, its value can be brought up to 30 yuan/N, is equivalent to SO
2Value reach 400～500 yuan/ton, perhaps the value of the sulphur in the coal reaches 800～1000 yuan/ton.Therefore, be that the FGD technology of raw material can produce tangible economic worth with ammonia.
This technology especially has application prospect in China.China is a population, grain and chemical fertilizer big country, and the output of chemical fertilizer is converted into synthetic ammonia, is equivalent to 3,500 ten thousand tons/year.Can solve 1,500 ten thousand tons of SO with the FGD technology
2/ year calculate, 8,000,000 tons/year of synthetic ammonia need be provided, account for aggregate demand 1/4th a little less than.In addition, carbon ammonium or urea only contain nitrogen nutrition, and nitrogenous and sulphur nutrition simultaneously in the sulphur ammonium.Therefore, the sulphur ammonium is than carbon ammonium and the better chemical fertilizer of urea, has huge market prospects in China.
But ammonia process is had relatively high expectations to supply of raw material, and the accumulating difficulty of liquefied ammonia has limited its development to a certain extent.
The magnesium method generally is raw material with magnesia, also can magnesium carbonate, or the mixture that contains magnesium carbonate and calcium carbonate is a raw material.Compare with the calcium method, the advantage of magnesium method is that the solubility (10g/L) of magnesium sulfite in water is 300 times of calcium sulfite (0.03g/L), and under the similarity condition, the absorption liquid internal circulating load of magnesium method is more much lower than calcium method.But the price of raw material is generally than calcium method height, and the purposes of sulphur removal product magnesium sulfate is less.Thereby, be positioned at longshore power plant and can adopt this method, because the sulphur removal product can directly enter the sea with aqueous solution form.
Therefore, existing method respectively has its pluses and minuses.But they have any is identical, is exactly the cleaning equipment that all has a structural similarity, or claims purifying column and desulfurizing tower.Desulfurizing tower is a very typical gas-liquid mass transfer (contact) equipment.In technical field of chemical engineering, be called the chemical absorbing tower, the solute in the gas phase (pollutant is such as sulfur dioxide etc.) is dissolved in the liquid phase, with the alkaline absorbent generation chemical reaction in the liquid phase, is transformed into a kind of new material.
At chemical field, at first the absorption tower form of Xuan Zeing is a packed tower, and the gas-liquid mass transfer surface is provided by filling surface, and next adopts the plate column structure, and the gas-liquid mass transfer surface is the foam surface that the gas bubbling forms.These two kinds of turriforms are suitable for clean system, such as not containing solid and being difficult for the system that obstruction takes place structure.For process such as the waste gas sulphur removal, no matter above which kind of method, all exist easy blocking problem, not because the waste gas dust-laden, be exactly that intermediate product is insoluble, end product crystallization etc. because raw material is insoluble, thereby the packed tower of extensive use and board-like tower are difficult to adapt to waste gas sulphur removal process in general chemical process.
But, prior art has a distinct disadvantage to be, the waste gas that temperature is higher, the EGT that has surpasses 200 ℃, enters the sulphur removal purifying column from sulphur removal purifying column bottom, and promptly exhaust gas inlet is in the bottom of sulphur removal purifying column, cause sulphur removal purification tower major part to be in the high temperature damage district, anticorrosion requirement and handling safety requirement for the sulphur removal purifying column are very high, the general all necessary huge circulating fluid flow that adopts, and energy consumption is also big.Because present sulphur removal purifying column all adopts the method for carbon steel liner rubber or lining resin scale to be made, these inner lining material heatproofs generally are no more than 70 ℃, and are difficult to overcome the long-term fluctuation of operational load, and inner liner comes off easily, and is not wear-resistant.More be not easy to adopt fiberglass reinforced plastics (FRP), be called for short fiberglass.Therefore, the difficult material of selecting fiberglass as the sulphur removal purifying column of prior art.
In addition, prior art also exists an improved place of needs to be, the sulphur removal process becomes the sulphite except absorbing sulfur dioxide, must be sulfate with sulfite oxidation also, and sulfate precipitation is come out.First process is called absorption, and second process is called oxidation, and the 3rd process is called crystallization.Early stage technology is that three processes are separately carried out in different equipment, and is perhaps interval in the difference of same equipment.This has also increased the complexity of desulfurizing tower structure.
Therefore, how to improve the structure of desulfurizing tower, regulate and control effectively the operating temperature of desulfurizing tower distribution (as, design a kind of new equipment, make the high-temperature region be positioned at the higher position, high-temp waste gas at first enters the high-temperature region; Low-temperature space is positioned at lower position, and the cooling purified waste gas arrives low-temperature space downwards), make it can adopt glass-reinforced plastic material; And three main processes of reasonable disposition are efficiently carried out its major part (for example oxidation and crystallization) or whole (absorption, oxidation and crystallization) in same desulfurizing tower, thereby reduction equipment investment, reducing can be good, the security of raising equipment operation, and operating flexibility, be existing waste gas purification, especially sulfur removal technology develops and an improved important directions.
Summary of the invention
The utility model technical issues that need to address are to disclose a kind of new off-gas cleaning equipment, and corollary apparatus, also relate to relevant process innovation, relate in particular to a kind of waste gas sulphur removal purifying column and corollary apparatus thereof, to overcome the above-mentioned defective that prior art exists.
Technology contents of the present utility model is as follows:
It at first relates to a kind of waste gas two step sulphur removal methods of purification, wherein, the first step, the high position washing of waste gas absorbs, and it comprises three processes: (1) mass-transfer progress, the washing absorption liquid carries out chemical absorbing to the gaseous contaminants such as sulfur dioxide in the waste gas; (2) dust washing process, the washing absorption liquid carries out the physics washing to the solid contaminant in the waste gas; (3) the decreasing temperature and increasing humidity process of waste gas, the steam in the washing absorption liquid is to the waste gas transmission, and the heat of waste gas is to the absorption liquid transmission simultaneously.Second step, the low level processing of washing absorption liquid, it comprises three processes: the separating of the oxidation of sulphite, the saturated crystallization of sulfate and solid, and the Recycling Mother Solution that separates behind the solid is carried out reuse to the first step.
The general designs that realize the industrial equipment of the above-mentioned two step sulphur removal methods of purification are: the equipment of developing various solid waste and various waste gas in a kind of washing, purifying waste gas, comprise washing absorption component and separating member, it is characterized in that, the washing absorption component is positioned at the higher high temperature cavity volume in position, separating member is positioned at the lower low temperature cavity volume in position, and the former exhaust gas entrance of high temperature is arranged on described high temperature cavity volume.Promptly, at higher height and position (being called for short high-order) a washing absorbent assembly is set, this assembly can absorb the solid particle discarded object, also can absorb pernicious gas, especially comprising that an akaline liquid that absorbs oxysulfide waste gas discharges scatters device, and the pH value of spray droplet is greater than 6 the washing absorption liquid dispersion device that distributes under the preferred high-temp waste gas environment.The distribution that this washing absorbent assembly also can comprise the washing absorbing medium of other pernicious gases such as NOx, HCl and HF in addition disperses device.
Waste gas at first enters above-mentioned washing absorbent assembly, enters the separation assembly that lower height and position (abbreviation low level) is provided with then, and the latter can realize that circulation is connected with above-mentioned washing absorbent assembly.In this case, separation assembly can be called cleaning absorbing circulation component.Separation assembly or cleaning absorbing circulation component can be used for the separation of solid particle discarded object, and the processing of pernicious gas chemical treatments, for example oxidation, separate out, crystallization, separation etc.
Cleaning absorbing circulation component also can be remaining washing absorption liquid, perhaps the same distribution of other washing absorbing medium recycled back washing absorbent assemblies disperses device, perhaps disperses device according to the classification enforcement classification of washing absorbing medium, the different distributions that the washing absorbent assembly is sent in classification back to.
Preferred version of the present utility model is that the main body of above-mentioned washing absorbent assembly, cleaning absorbing circulation component all is arranged in the same tower body, between the tower chamber that two assemblies occupy respectively the rectangular flue interface is set.
Waste gas after the purification can be from the outlet of the bottom, tower chamber that last assembly occupies, and perhaps the outlet from the top, tower chamber that next assembly occupies enters the flue interface that is provided with therebetween.
Therefore, on waste gas sulphur removal purifying column of the present utility model, exhaust gas inlet is arranged on the top of tower, high temperature raw material waste gas is advanced from sulphur removal purifying column top, also flow downwards with the washing absorption liquid that comprises alkaline sulphur removal raw material, at high level, waste gas is lowered the temperature, the purification of humidification, sulphur removal and other polluters.After the waste gas sulphur removal purifies, get rid of the sulphur removal purifying column from low level.Like this, make the EGT extreme higher position be in the highest order place of purifying column, the i.e. top of tower, all the other positions, especially low portion all is a low-temperature space, and for adopting the not high plastic material of tolerable temperature, especially glass fiber reinforced plastic material is made purifying column very favorable condition is provided.Consequently, not only guarantee high sulphur removal and purification efficiency, also significantly reduced the height of sulphur removal purifying column, simplified the complexity of sulphur removal and cleaning system.
What deserves to be explained is that the said and stream motion of the utility model is meant that mainly high temperature raw material waste gas enters from sulphur removal purifying column 1 top, also flows with liquid that comprises sulfur elimination or gas downwards.
And the end that the utility model said " top " is any equipment or device, is the optional position of side in the heart, and for example, two ends are spherical cylindrical tower body about in the of one, and its " top " is other any positions outside the spherical position, lower end.Certainly, if spherical position, lower end is bigger, and, the bottommost of spherical position, lower end is provided with container, the utility model said " top " can be can be regarded as in any position of this container top so, comprises that the upper position of lower end spherical part is also calculated " top ", and the exhaust gas inlet at " top " can be arranged on this upper position, the perhaps optional position of cylinder, perhaps any position of upper end spherical member.
Secondly, the sulphur removal purifying column can be divided into two sections, have different functions, epimere is called the washing absorber portion, deviates from the polluter in the waste gas, comprises sulfur dioxide, generates sulphite; Hypomere is called the absorption liquid canned paragraphs, and its function is to store absorption liquid, as circulating slot, sulfite is oxidized to sulfate, finishes sulphate crystal simultaneously, therefore, is also referred to as the oxidizing and crystallizing device.
Test shows, according to device of the present utility model and stream or the exhaust gas purifying method design of two step of following current,
(1) for ammonia process; can obtain sulfur acid ammonium liquid, slurry, worry cake; particle or crystal product; wherein; the water content of ammonium sulfate liquid is no more than 80%, and the water content of ammonium sulfate slurry is no more than 50%, and the humidity of considering cake is less than 10%; the granularity of sulfur acid ammonium grain products is between 0.05～0.5mm, and the purity of ammonia sulfate crystal reaches 90～99%.
(2), can obtain to contain slurry, the worry cake of dihydrate gypsum, particle or crystal product for the calcium method; wherein, the gypsum content of gypsum slurry is not less than 5%, and the gypsum content of considering cake is greater than 80%; the granularity of gypsum-containing products is between 0.05～0.15mm, and purity reaches 90～95%.
(3) for the magnesium method; can obtain sulfur acid magnesium liquid, slurry, worry cake; particle or crystal product; wherein; the water content of magnesium sulfate liquid is no more than 80%, and the water content of magnesium sulfate slurry is no more than 50%, and the humidity of considering cake is less than 10%; the granularity of sulfur acid magnesium granules product is between 0.05～0.5mm, and the purity of the epsom salt of crystal reaches 90～99%.
General implementation method of the present utility model and process matched therewith device are as follows:
Temperature is 100～200 ℃, contain SO
2Concentration is 200～20000mg/Nm
3Waste gas, deliver to the exhaust gas inlet at sulphur removal purifying column 1 top by booster fan 2, (absorption liquid contains alkaline matter with absorption liquid, abbreviation sulphur removal raw material) the contact temperature is reduced to 55～65 ℃, enters the washing absorber portion, and acidic materials and the alkaline matter in the absorption liquid in the waste gas generate corresponding salt, such as sulfate, nitrate, chloride and fluoride etc., SO
2Form sulphite with the sulfur elimination reaction in the absorption liquid, such as ammonium sulfite, calcium sulfite, perhaps magnesium sulfite, EGT further is reduced to 45～55 ℃ simultaneously, and the waste gas after the purification leaves sulphur removal purifying column 1 from sulphur removal purifying column middle part, enters demister 8, after removing the liquid foam of deentrainment, enter smoke stack emission;
Generally, waste gas and absorption liquid enter the sulphur removal purifying column from top, and stream, or following current is downward;
Absorption liquid takes out from the absorption liquid canned paragraphs (also double as is the circulating slot of absorption liquid) of hypomere, is transported to through circulating pump 6, and sulphur removal purifying column 1 epimere forms fine drop through the spray thrower atomizing, enters the washing absorber portion from top to down, absorbs the SO in the waste gas
2After other component, enter the oxidizing and crystallizing device of sulphur removal purifying column bottom, at the absorption liquid canned paragraphs, the air oxidation that the oxidized air-blaster 7 of sulphite blasts is a sulfate, separate out the sulphate crystal body in the concentration of sulfate above under its solubility situation simultaneously, form the liquid of pulpous state;
The sulfate liquid of pulpous state is discharged from sulphur removal purifying column 1 bottom, and through circulating pump 6, most of with additional sulfur elimination converges the back circulation and enters sulphur removal purifying column 1, and fraction enters slurry concentrator 3, obtains two strands of slurries: underflow material and grout.Grout turns back to sulphur removal purifying column 1, and the underflow material enters solid-liquid separator 4, obtains mother liquor and solid sulfate salt.Mother liquor also turns back to sulphur removal purifying column 1, and solid enters back processing unit (plant) 5, such as drier or granulating and drying device.
Said sulphur removal raw material is any one material that presents alkalescence in the aqueous solution, and typically this class material has lime stone, or claims calcium carbonate, and derivative, such as calcium oxide; Ammonia, its form can be the ammonia of liquefaction, carbonic hydroammonium, or ammonia/aqueous mixtures, and gaseous ammonia; Magnesia or magnesium carbonate.
The sulphur removal raw material can directly be added the absorption liquid canned paragraphs at purifying column 1, also can be added on the circulation line, can be on the inlet ductwork of circulating pump 6, and also can be on the export pipeline of circulating pump 6.The flow size of sulphur removal raw material is generally adjusted according to the sulfur dioxide load of waste gas and the pH value of absorption liquid.The deamination district is being set, promptly be provided with on the basis in sulphur removal district under the situation in deamination district, the incoming interface that adds of preferred sulfur elimination ammonia is arranged on the sulphur removal pipeloop, be not arranged on the tower body, be not arranged on the deamination circulation line that may add setting yet, purpose is to allow the free ammonia content in the deamination circulating absorption solution is reduced to minimum level, the deamination district is become with the absorption of ammonia and the simultaneous zone of absorption of sulfur dioxide, even be absorbed as main zone with ammonia, reduce the ammonia loss by volatilization in the tail gas to greatest extent.
The water of waste gas decreasing temperature and increasing humidity and sulphur removal reaction needed is called fresh water (FW), and mainly the washing mouth from demister 8 enters, and its flow size is generally adjusted according to the liquid level of purifying column.
The device of realizing said method comprises cleaning equipment, and this equipment comprises:
Cross section is the tower body of circle or rectangle;
Be arranged on the former exhaust gas inlet of high temperature of a tower body high position;
Be arranged on the washing absorber portion in the tower body high position;
Be arranged on the absorption liquid distributor of washing absorber portion;
Be arranged on the absorption liquid canned paragraphs in the tower body low level;
Be arranged on the oxidation air distributor in the absorption liquid canned paragraphs, as the oxidative function element of sulphite;
Be arranged on the agitator in the absorption liquid canned paragraphs, both strengthened element, also strengthen element, also suspend and avoid depositing the element of caking as solid as sulphate crystal as oxidation;
Be arranged on the tower body waste gas outlet between washing absorber portion and the absorption liquid canned paragraphs;
Especially, the material of tower body is a fiberglass reinforced plastics, or fiberglass, and Corrosion Protection is good, short construction period.
And the absorption liquid distributor comprises a house steward, and some arms that link to each other with house steward, with the nozzle that is connected with arm.The flowing velocity of absorption liquid in pipe is 1.5～2.5m/s.At least seven nozzles of absorption liquid distributor configuration, and the spout of at least one is towards exhaust gas inlet, preferably all towards exhaust gas inlet.Desired nozzle is a spiral nozzle, and the rotation number of turn of spiral is 2～5 circles.The spout internal diameter of spiral nozzle is between 20～100mm.The distribution density of nozzle number is that the basis is 1～3 nozzle/m with the cross-sectional area of corresponding region
2The sprinkle density of desired absorption liquid based on the cross-sectional area of correspondence, is 20～200m
3/ m
2/ h.
The diameter of absorption liquid canned paragraphs be the washing absorber portion diameter 1.0-2.0 doubly, the height of washing absorber portion be the washing absorber portion diameter 0.75-2.0 doubly, the height of absorption liquid canned paragraphs be the absorption liquid canned paragraphs diameter 0.75-2.0 doubly.
The characteristics of this purifying column are that waste gas and absorption liquid all enter from the top of tower, and whole flowing is and flows to current downflow, the mass-transfer efficiency height, and the exhaust-gas treatment ability is big.
Adopt the purifying column of said structure to be used for waste gas purification, the eliminating efficiency of polluter can reach 95～99%.Purifying column of the present utility model, simple in structure, disposal ability is big, and the absorption liquid flow is little, and absorption liquid also flows in the same way with waste gas and contacts, and more helps improving exhaust gas velocity, strengthens mass transfer velocity, reduces tower diameter, lowers investment.
In addition, when waste gas SO2 absorbs, wash when also being accompanied by other polluters and remove, such as SO
3, NO
2, HF and HCl, the compound of mercury and coal ash dirt, therefore, purifying column of the present utility model has the effect that the multi-pollutant kind removes simultaneously.
What be worth reaffirming is, the lower part of purifying column is divided into absorption liquid canned paragraphs (105), and its function is the liquid of collecting to get off from washing absorber portion (103), also can be used as the circulating slot of absorption liquid circulation.The canned paragraphs (105) of washing absorption liquid has the function of the aqueous solution drum air oxidation of sulphite, and the crystallization function after the sulfate supersaturation, and in canned paragraphs (105), be provided with the enhancing element that at least one agitator (106) and at least one air sparger (107) suspend as oxidation, crystallization and solid.
The device of realizing said method also comprises at least one waste gas booster fan 2, at least one sulfate slurry inspissator 3, at least one solid-liquid separator 4, at least one sulfate solid processing unit (plant) 5, at least one slurry circulating pump 6, at least one oxidation air air blast 7 and at least one demister 8.
Solid-liquid separator 4 can adopt press type, centrifugal or vacuum type, for ammonia process and magnesium method, preferentially adopt centrifugal, for the limited employing vacuum type of calcium method.
Sulfate solid processing unit (plant) 5 comprises the drying of sulfate, or granulation and drying, and packaging facilities.For the calcium method, preferentially adopt granulation, drying and roasting apparatus, preferentially adopt drying equipment for ammonia process, for the magnesium method, preferentially adopt drying and roasting apparatus.
Description of drawings
Fig. 1 is the Tower for purifying waste gas structural representation.
Fig. 2 is the process matched therewith installation drawing.
The specific embodiment
Referring to Fig. 1, method of the present utility model comprises the steps:
Contain SO
2Flue gas, temperature is 100～200 ℃, at first be sent to the top exhaust gas inlet of purifying column, enter the washing absorber portion of washing, purifying tower, contact closely with the fine drop that sprays out from the absorption liquid distributor, three processes take place simultaneously: (1) mass-transfer progress, the acid pollution material in the waste gas comprises SO
2, SO
3, NO
2, HCl, HF etc. are absorbed and enter absorption liquid, with the alkali substance reaction in the absorption liquid, become corresponding salt; (2) dust washing process, the solid matter in the waste gas such as the coal ash flue dust, specifically comprises aluminium oxide, silica, iron oxide etc. also are washed in the absorption liquid; (3) the decreasing temperature and increasing humidity process of waste gas is equivalent to caloic simultaneous interpretation process, and the steam in the absorption liquid is to the waste gas transmission, and the heat of waste gas causes EGT to reduce and the moisture content increase to the absorption liquid transmission simultaneously, and the minimizing of absorption liquid water content, promptly is concentrated.Behind the washing absorber portion, the eliminating efficiency of the vapor phase contaminants in the waste gas reaches 95-99%, and the dust detersive efficiency is at 70-90%, and temperature is reduced to 50-55 ℃.Then, waste gas leaves washing, purifying tower 1 from the waste gas outlet at middle part, enters demister 8 again and removes the liquid foam of carrying secretly in the waste gas, enters smoke stack emission again.
Absorption liquid enters from purifying column top, from top to down, absorbs the pollutant in the waste gas, especially enters the absorption liquid canned paragraphs of purifying column bottom behind the sulfur dioxide.At the absorption liquid canned paragraphs, the air oxidation that the sulphite that obtains from the washing absorber portion is blasted is a sulfate, the continuous cumulative rises of the concentration of sulfate, after surpassing solubility, can crystallization separate out solid, therefore, also be provided with air sparger and mixer in the oxidizing and crystallizing section, both increased the mass transfer of airborne oxygen, and promoted crystal growth again and prevent that deposition of solid is on base plate.
The sulfate liquid of pulpous state is discharged from sulphur removal purifying column 1 bottom, and through circulating pump 6, most of with additional sulfur elimination converges the back circulation and enters sulphur removal purifying column 1, and fraction enters slurry concentrator 3, obtains two strands of slurries: underflow material and grout.Grout turns back to sulphur removal purifying column 1, and the underflow material enters solid-liquid separator 4, obtains mother liquor and solid sulfate salt.Mother liquor also turns back to sulphur removal purifying column 1, and solid enters back processing unit (plant) 5, such as drier or granulating and drying device.
Said sulphur removal raw material is any one material that presents alkalescence in the aqueous solution, and typically this class material has lime stone, or claims calcium carbonate, and derivative, such as calcium oxide; Ammonia, its form can be the ammonia of liquefaction, carbonic hydroammonium, or ammonia/aqueous mixtures, and gaseous ammonia; Magnesia or magnesium carbonate.
The sulphur removal raw material can directly be added the absorption liquid canned paragraphs at purifying column 1, also can be added on the circulation line, can be on the inlet ductwork of circulating pump 6, and also can be on the export pipeline of circulating pump 6.The flow size of sulphur removal raw material is generally adjusted according to the sulfur dioxide load of waste gas and the pH value of absorption liquid.
The water of waste gas decreasing temperature and increasing humidity and sulphur removal reaction needed is called fresh water (FW), and mainly the washing mouth from demister 8 enters, and its flow size is generally adjusted according to the liquid level of purifying column.
Referring to Fig. 1, said purifying column 1 comprises:
Cross section is the tower equipment of circle or rectangle, i.e. tower body (101);
Be arranged on the exhaust gas inlet (102) at tower body top;
Be arranged on the washing absorber portion (103) of tower body internal upper part;
Be arranged on the absorption liquid distributor (104) of washing absorber portion;
Be arranged on the absorption liquid canned paragraphs (105) of tower body inner bottom part;
Be arranged on the agitator (106) in the absorption liquid canned paragraphs, both strengthened element, also strengthen element, also suspend and avoid depositing the element of caking as solid as sulphate crystal as oxidation;
Be arranged on the oxidation air distributor (107) of absorption liquid canned paragraphs, as the oxidative function element of sulphite;
Be arranged on the tower body waste gas outlet (108) between washing absorber portion and the absorption liquid canned paragraphs;
Especially, the material of tower body is a fiberglass reinforced plastics, or fiberglass, and Corrosion Protection is good, short construction period.
In addition, in order to reduce the tower body height, save material and investment, waste gas outlet (108) is a rectangle or approximate rectangular.
And, the diameter of absorption liquid canned paragraphs (105) be washing absorber portion (103) diameter 1.0-2.0 doubly, the height of washing absorber portion (103) be washing absorber portion (103) diameter 0.75-2.0 doubly, the height of absorption liquid canned paragraphs (105) be absorption liquid canned paragraphs (105) diameter 0.75-2.0 doubly.
Embodiment 1
Flue-gas flow rate is 500,000 Nm
3/ hr, SO
2Content is 3200mg/Nm
3, the content of other pollutants is in the waste gas: dirt=80mg/Nm
3, SO
3=55mg/Nm
3, HCl=35mg/Nm
3, HF=20mg/Nm
3, NOx=100mg/Nm
3, EGT is 120 ℃.
This embodiment is adopted ammonia process sulphur removal and purification, and the sulphur removal raw material is 18% ammonia water mixture for the ammonia weight concentration, and the sulphur removal byproduct is an ammonium sulfate.This washing purifying device mainly comprises following equipment: 3 (being made up of hydrocyclone, centrifuge and drying machine) of booster fan 2, purifying column 1, circulating pump 6 (also can be standby), a cover sulphur ammonium dewater unit, an oxidation fan 5 (also can be standby) and be arranged in the interior demister 8 of exhaust pass.
Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.
The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.
The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is regulated by adding fresh water (FW) to the demister flushing pipe, and liquid level is controlled at 10.5m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows:
SO
2＝97.8％，SO
3＝100％，HCl＝100％。HF=100%, NOx=22.5%, dirt=89%.
The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 14.8%, behind over cure ammonium dewater unit 3, be met the thiamine fertilizer product of national standard, nitrogen content is 20.9, water content is 0.4%, and production capacity is 3.36 tons/hour.
Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 50.5 ℃.
Embodiment 1 is adopted calcium method sulphur removal and purification, and the sulphur removal raw material is the lime stone through pulverizing and grinding, and granularity greater than 90%, is mixed with the lime stone solid content and is 15% lime stone slurry less than 325 purposes.
The sulphur removal byproduct is a dihydrate gypsum, CaSO4.2H
2O.
Capital equipment configuration is as follows: booster fan 2, purifying column 1, circulating pump 6 (also can be standby), a cover sulphur ammonium dewater unit 3 (being made of hydrocyclone and vacuum filter), an oxidation fan 5 (also can be standby) and be arranged in demister 8 in the exhaust pass.
The size of purifying column 1 is identical with embodiment 1.Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is added fresh water (FW) by body from the demister flushing pipe and is regulated, and liquid level is controlled at 10.5m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows: SO
2=96.5%, SO
3=99.5%, HCl=100%, HF=100%, NOx=24.5%, dirt=93%.The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 13.5%, through behind the dewater unit 3, obtains gypsum by-product, and water content is 8.5% in the gypsum, and production capacity is 4.7 tons/hour.Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 50.3 ℃.
Embodiment 1 is adopted magnesium method sulphur removal and purification, and the sulphur removal raw material is a magnesia, and granularity greater than 90%, is mixed with solid content and is 15% magnesia slurries less than 150 purposes.The sulphur removal byproduct is an epsom salt, MgSO4.7H
2O.
Capital equipment configuration is as follows: booster fan 2, purifying column 1, circulating pump 6 (also can be standby), a cover sulphur ammonium dewater unit 3 (by hydrocyclone and centrifuges), an oxidation fan 5 (also can be standby) and be arranged in demister 8 in the exhaust pass.
The size of purifying column 1 is identical with embodiment 1.
Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.
The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.
The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is added fresh water (FW) by body from the demister flushing pipe and is regulated, and liquid level is controlled at 10.5m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows: SO
2=96.5%, SO
3=99.5%, HCl=100%, HF=100%, NOx=24.5%, dirt=93%.
The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 16.5%, through behind the dewater unit 3, obtains the magnesium sulfate byproduct, and water content is 4.5%, and production capacity is 6.47 tons/hour.
Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 50.5 ℃.
Embodiment 4
Flue-gas flow rate is 1,200,000 Nm
3/ hr, SO
2Content is 9000mg/Nm
3, the content of other pollutants is in the waste gas: dirt=220mg/Nm
3, SO
3=105mg/Nm
3, HCl=35mg/Nm
3, HF=20mg/Nm
3, NOx=500mg/Nm
3, EGT is 135 ℃.
This embodiment is adopted ammonia process sulphur removal and purification, and the sulphur removal raw material is a liquefied ammonia, and the sulphur removal byproduct is an ammonium sulfate.
This washing purifying device mainly comprises following equipment: 3 (being made up of hydrocyclone, centrifuge and drying machine) of purifying column 1, two circulating pumps 6 (also can be standby), a cover sulphur ammonium dewater unit, two oxidation fans 5 (also can be standby) and be arranged in the interior demister 8 of exhaust pass.
Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.
The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.
The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is added fresh water (FW) by body from the demister flushing pipe and is regulated, and liquid level is controlled at 15.0m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows: SO
2=98.8%, SO
3=100%, HCl=100%.HF=100%, NOx=28.5%, dirt=91%.The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 15.8%, behind over cure ammonium dewater unit 3, be met the thiamine fertilizer product of national standard, nitrogen content is 20.85, water content is 0.42%, and production capacity is 22.72 tons/hour.
Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 52.5 ℃.
Embodiment 4 is adopted calcium method sulphur removal and purifications, and the sulphur removal raw material is the lime stone through pulverizing and grinding, and granularity greater than 90%, is mixed with the lime stone solid content and is 15% lime stone slurry less than 325 purposes.
The sulphur removal byproduct is a dihydrate gypsum, CaSO4.2H
2O.
Capital equipment configuration is as follows: purifying column 1, three circulating pumps 6 (also can be standby), a cover sulphur ammonium dewater unit 3 (being made of hydrocyclone and vacuum filter), two oxidation fans 5 (also can be standby) and be arranged in demister 8 in the exhaust pass.
The size of purifying column 1 is identical with embodiment 4.
Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.
The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.
The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is added fresh water (FW) by body from the demister flushing pipe and is regulated, and liquid level is controlled at 10.5m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows:
SO
2=97.8%, SO
3=99.7%, HCl=100%, HF=100%, NOx=32.5%, dirt=94%.
The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 14.5%, through behind the dewater unit 3, obtains gypsum by-product, and water content is 8.8% in the gypsum, and output is 31.83 tons/hour.
Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 52.3 ℃.
Embodiment 4 is adopted magnesium method sulphur removal and purifications, and the sulphur removal raw material is a magnesia, and granularity greater than 90%, is mixed with solid content and is 15% magnesia slurries less than 150 purposes.
The sulphur removal byproduct is an epsom salt, MgSO4.7H
2O.
Capital equipment configuration is as follows: purifying column 1, two circulating pumps 6 (also can be standby), a cover sulphur ammonium dewater unit 3 (by hydrocyclone and centrifuges), two oxidation fans 5 (also can be standby) and be arranged in demister 8 in the exhaust pass.
The size of purifying column 1 is identical with embodiment 1.
Purifying column 1 tower body 101 adopts fiberglass reinforced plastics, i.e. glass-reinforced plastic material manufacturing.
The sulphur removal raw material is added on the inlet of circulating pump pipeline, by mixing with circulating absorption solution behind the impeller of pump.
The liquid level of purifying column 1 bottom absorption liquid canned paragraphs 105 is added fresh water (FW) by body from the demister flushing pipe and is regulated, and liquid level is controlled at 10.5m.The pH of absorption liquid controls by the flow of regulating the sulphur removal raw material, is controlled between the 5.0-5.5.
Through behind the purifying column, the purification efficiency of each pollutant is as follows:
SO
2=98.8%, SO
3=99.6%, HCl=100%, HF=100%, NOx=24.5%, dirt=92%.
The bottom absorption liquid canned paragraphs of purifying column 1, promptly in the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 16.5%, through behind the dewater unit 3, obtains the magnesium sulfate byproduct, and water content is 4.5%, and production capacity is 43.46 tons/hour.
Waste gas after the purification leaves purifying column 1, enters the demister 8 that places exhaust pass, enters smoke stack emission except that behind the liquid foam of deentrainment, and its temperature is 51.8 ℃.
Claims (10)
1. waste gas purification apparatus, comprise a cleaning equipment (1), and the washing absorber portion (103) and the absorption liquid canned paragraphs (105) that are arranged on described cleaning equipment (1) inside, it is characterized in that, washing absorber portion (103) is positioned at the high position of described cleaning equipment (1), absorption liquid canned paragraphs (105) is positioned at the low level of described cleaning equipment (1), and also is provided with the former exhaust gas inlet of high temperature (102) in the high position of described cleaning equipment (1).
2. waste gas purification apparatus according to claim 1, it is characterized in that, the diameter of absorption liquid canned paragraphs (105) be washing absorber portion (103) diameter 1.0-2.0 doubly, the height of washing absorber portion (103) be washing absorber portion (103) diameter 0.75-2.0 doubly, the height of absorption liquid canned paragraphs (105) be absorption liquid canned paragraphs (105) diameter 0.75-2.0 doubly.
3. waste gas purification apparatus according to claim 1 is characterized in that, described washing absorber portion (103) comprises washing absorption liquid distributor (104), at least seven nozzles of described washing absorption liquid distributor (104) configuration.
4. waste gas purification apparatus according to claim 3 is characterized in that, the spout of at least one nozzle is towards the former exhaust gas inlet of described high temperature (102) in the described nozzle.
5. waste gas purification apparatus according to claim 3, it is characterized in that, described washing absorption liquid distributor (104) comprises a house steward, and some arms that link to each other with house steward, with the nozzle that is connected with arm, the absorption liquid flowing velocity of house steward and arm is 1.5～2.5m/s, desired nozzle is a spiral nozzle, the rotation number of turn of spiral is 2～5 circles, the spout internal diameter of spiral nozzle is between 20～100mm, the distribution density of nozzle number is 1～3 nozzle/m based on the cross-sectional area of corresponding region
2, the sprinkle density of desired absorption liquid based on the cross-sectional area of correspondence, is 20～200m
3/ m
2/ h.
6. waste gas purification apparatus according to claim 1 is characterized in that, the waste gas outlet behind the washing, purifying (108) is arranged on the below of described washing absorber portion (103) and the top of described absorption liquid canned paragraphs (105).
7. waste gas purification apparatus according to claim 6 is characterized in that, described absorption liquid canned paragraphs (105) comprises at least one agitator (106) and at least one oxidation air distributor (107).
8. waste gas purification apparatus according to claim 1 is characterized in that, described cleaning equipment (1) connects at least one oxidation air air blast (7), at least one circulating pump (6), at least one demister (8), and at least one slurry concentrator (3).
9. waste gas purification apparatus according to claim 8 is characterized in that, washing absorbs adding on the circulation line that inlet is arranged on the washing absorption liquid of raw material, also can be arranged on the inlet ductwork of circulating pump (6) or on the export pipeline.
10. waste gas purification apparatus according to claim 8 is characterized in that, described slip inspissator (3) connects at least one solid-liquid separator (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200589482U CN201195095Y (en) | 2008-05-26 | 2008-05-26 | Waste gas purifier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200589482U CN201195095Y (en) | 2008-05-26 | 2008-05-26 | Waste gas purifier |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201195095Y true CN201195095Y (en) | 2009-02-18 |
Family
ID=40414735
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008200589482U Expired - Fee Related CN201195095Y (en) | 2008-05-26 | 2008-05-26 | Waste gas purifier |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201195095Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110449003A (en) * | 2019-08-09 | 2019-11-15 | 苏州匹丝软件设计有限公司 | A kind of gaseous state flue gas desulphurization unit |
| CN110813032A (en) * | 2019-09-28 | 2020-02-21 | 中国人民解放军63605部队 | Intelligent self-regulation and control absorption device for dinitrogen tetroxide waste liquid |
-
2008
- 2008-05-26 CN CNU2008200589482U patent/CN201195095Y/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110449003A (en) * | 2019-08-09 | 2019-11-15 | 苏州匹丝软件设计有限公司 | A kind of gaseous state flue gas desulphurization unit |
| CN110813032A (en) * | 2019-09-28 | 2020-02-21 | 中国人民解放军63605部队 | Intelligent self-regulation and control absorption device for dinitrogen tetroxide waste liquid |
| CN110813032B (en) * | 2019-09-28 | 2022-05-27 | 中国人民解放军63605部队 | Intelligent self-regulation and control absorption device for dinitrogen tetroxide waste liquid |
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