CN101100301A - Device for producing ammonium sulfate - Google Patents
Device for producing ammonium sulfate Download PDFInfo
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- CN101100301A CN101100301A CNA2007101302189A CN200710130218A CN101100301A CN 101100301 A CN101100301 A CN 101100301A CN A2007101302189 A CNA2007101302189 A CN A2007101302189A CN 200710130218 A CN200710130218 A CN 200710130218A CN 101100301 A CN101100301 A CN 101100301A
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Abstract
This invention relates to an installation for producing ammonium sulfate by using sulphur dioxide from waste-gas as raw material. It is a novel sulphur dioxide absorption tower, which is composed of three functional zones: ammonia-removing, sulphur-removing and oxidation/crystallizing. From the top to the bottom, equipped are: a flue gas vent; a liquid/gas separator of washing water distributor; an ammonia-removing absorption liquid distributor connected with circulation absorption liquid inlet; an ammonia-removing zone; a sulphur-removing circulation absorption liquid (SRCAL) distributor connected with SRCAL inlet; a sulphur-removing zone; an over-flow outlet is place don the tower; below which is oxidation/crystallizing zone. The advantages of this invention are: low investment, low energy-consumption, high treatment ability, high efficiency, suitable for commercial application.
Description
Technical field
This invention belongs to clean energy technology and clean coal technology field, is mainly used in heat power station, industrial coal or oil-firing boiler, and the SO of metallurgical mineral sinter machine waste gas
2The waste gas reclaiming clean.Also can belong to chemical industry and environmental protection field.
Background technology
With coal or oil is the boiler or the fuel-burning power plant discharging large quantity of exhaust gas of fuel.These waste gas contain objectionable impuritiess such as SOx, NOx, HCl and HF, and wherein SOx is the essential substance that forms acid rain.With the difference of burning coal, SO
2Content is usually at 300～5000ppmv (1000～15000mg/Nm
3) between.But exhausted air quantity is very huge, and the opinion with coal firing 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 quantity dischargeds.Because SO
2Be sour gas, adopt alkaline aqueous solution to take off the SOx that inhales in the waste gas, i.e. (Flue Gas Desulfurization FGD) is effective means, is with a wide range of applications in waste-gas desulfurization.
Yet in the existing waste-gas desulfurization technology, what extensively adopt is the Wingdale～gypsum method (being also referred to as the calcium method) of raw material with the Wingdale still still, and its desulfuration byproduct is a gypsum.Because the purposes of gypsum is very limited, the gypsum of desulfurization by-product is to be distilled off as the master.Therefore, these class methods are called the method for abandoning.The method of abandoning has significant disadvantages: consume new natural resources; Waste gas becomes waste residue, brings new pollution; Discharge CO simultaneously
2, be greenhouse gases, and investment is big, the energy consumption height.
Synthetic ammonia is alkaline matter, and as sweetening agent, its desulfurization product is an ammonium sulfate, is called for short the sulphur ammonium, can be used as the agrochemical of high fertilizer efficiency.This method is called ammonia-process desulfurization technique.This method reclaims the sulfurous gas in the waste gas, the chemical fertilizer that the production added value is higher.
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 2,000 ten thousand tons of SO with the FGD technology
2/ year calculating need provide 1,000 ten thousand tons/year of synthetic ammonia, accounts for national synthetic ammonia aggregate demand less than 30%, can produce 4,000 ten thousand tons of ammonium sulfate, nearly 30,000,000,000 yuan of the output value simultaneously.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 outlook in China.But, China, so in the world wide, the output of ammonium sulfate is all very low, all is byproduct basically, does not almost have the factory that produces ammonium sulfate fertilizer specially.Therefore, development is based on the thiamine fertilizer industry of waste-gas desulfurization, for promoting that China's Agricultural Development is significant.
Three steps of ammonia-process desulfurization technique correspondence are as follows:
(1) SO
2Absorb, show as the acid-base reaction in the aqueous solution, at first generate ammonium sulphite, react as follows:
SO
2+ H
2O+2NH
3=(NH
4)
2SO
3(ammonium sulphite)
(2) sulfite oxidation is an ammonium sulfate, and chemical reaction also takes place in the aqueous solution, reacts as follows:
(NH
4)
2SO
3+ 1/2O
2=(NH
4)
2SO
4(ammonium sulfate)
(3) ammonium sulfate crystallization after the ammonium sulfate concentrations in the aqueous solution surpasses solubleness, can crystallization be separated out the solid ammonium sulfate particle.Crystallization also is looked at as a chemical reaction usually, that is:
(NH
4)
2SO
4(L, fluid sulphuric acid ammonium)=(NH
4)
2SO
4(S, solid ammonium sulfate).
But different with other alkaline matters is that ammonia is volatile.Traditional counter current contact formula absorption tower no matter be spray column, packing tower or tray column, is being positioned at the point of contact of top of tower, and ammonia concentration is the highest in the absorption liquid, and the middle mutually SO of gas
2Concentration is minimum.Therefore, the concentration of ammonia in gas phase will be the highest.This means that ammonia will be very big with the amount that tail gas overflows thionizer.The waste loss that this both can cause ammonia can cause new pollution again.This difficult problem causes ammonia-process desulfurization technique to fail a major reason of fine development in the past for a long time just.
Summary of the invention
For overcoming above-mentioned defective and the deficiency that prior art exists, the present invention has proposed a kind of new production equipment by waste gas sulfate ammonium, respectively shown in attached Fig. 1 and 2 from the angle of the volatilization loss of reduction ammonia.Accompanying drawing 1 is the device of this invention, the sulfurous gas absorption tower that accompanying drawing 2 comprises for this device.
By a kind of production method by waste gas sulfate ammonium of device design of the present invention, this method comprises three steps, and the single order ammonia process of desulfurization of former waste gas purifies; The second order deamination and desulfurization of half purifying exhaust air purifies; Described single order, second order are purified the ammonium sulfite solution that produces implement oxidizing and crystallizing.The device of realizing this method can be a kind of cylindrical or tower equipment of quadrate, abbreviates sulfurous gas absorption tower 1 as;
Sulfurous gas absorption tower 1 mainly is divided into three functional zone: deamination district 106, desulfurization zone 108 and oxidizing and crystallizing district 1010.
(1) the deamination district mainly finishes the task that ammonia reclaims, and the ammonia that the waste gas of deviating from most of sulfurous gas that comes from desulfurization zone contains is absorbed in this zone, further is absorbed in this zone at the remaining sulfurous gas of desulfurization zone simultaneously.This regional height is H1, and diameter is D1.The deamination district is positioned between deamination absorption liquid sparger and the desulfurization absorption liquid sparger.
(2) desulfurization zone is mainly finished the desulfurization task, and the sulfurous gas in the waste gas mainly is to be absorbed by liquid absorption at desulfurization zone to become ammonium sulphite.The height that this zone is positioned at is H2, and diameter is D2, between desulfurization absorption liquid sparger and overflow outlet.
(3) the absorption liquid that contains ammonium sulphite that gets off from desulfurization zone and deamination district directly falls into the oxidizing and crystallizing district.In this zone, the atmospheric oxidation that ammonium sulphite is blasted is an ammonium sulfate, and the ammonium sulfate concentrations in the absorption liquid is increased, and surpasses the saturation solubility of ammonium sulfate, and solid ammonium sulfate is separated out in crystallization.This regional height is H3, and diameter is D3, between overflow outlet and tower base plate.
As shown in Figure 1, the production equipment by waste gas sulfate ammonium of this invention includes, but are not limited to following equipment:
Sulfurous gas absorption tower (1);
Be arranged on the waste gas booster fan (2) of upstream, sulfurous gas absorption tower (1);
Be arranged on the oxidation air gas blower (3) of upstream, sulfurous gas absorption tower (1);
Be arranged near the deamination absorption liquid recycle pump (4) in sulfurous gas absorption tower (1);
Be arranged near the desulfurization absorption liquid recycle pump (5) in sulfurous gas absorption tower (1);
Be arranged on and advance ammonia mixing tank (6) on the absorption liquid circulation line that links to each other with desulfurization absorption liquid recycle pump (5);
The sulphur ammonium that is arranged on downstream, sulfurous gas absorption tower (1) extracts equipment (7);
Be arranged on gas, the liquid/gas separator wash-down water accumulator (8) of upstream, sulfurous gas absorption tower (1).
As shown in Figure 2, said sulfurous gas absorption tower (1) specifically comprises:
Be arranged on the purifying exhaust air outlet (102) of cat head, this outlet can be circular, also can be other shape.
Be arranged on gas, the liquid separating member (103) of tower body (101) internal upper part;
Be arranged on the wash-down water sparger (104) that is connected with water inlet in gas, the liquid separating member (103);
Be arranged on the deamination circulating absorption solution sparger (105) that is connected with the import of deamination circulating absorption solution of wash-down water sparger (104) below;
Be arranged on the deamination district (106) of deamination circulating absorption solution sparger (105) below;
Be arranged on the desulphurization circulating absorption liquid sparger (107) that is connected with the import of desulphurization circulating absorption liquid of below, deamination district (106);
Be arranged on the desulfurization zone (108) of desulphurization circulating absorption liquid sparger (107) below;
Be arranged on the exhaust gas entrance (1013) of desulfurization zone (108);
Be arranged on the oxidizing and crystallizing district (1010) of exhaust gas entrance (1013) below;
Be arranged on the air-distributor that is connected with gas inlet (1011) in oxidizing and crystallizing district (1010);
Be arranged on the agitator (1012) of air-distributor (1011) top or the bottom of oxidizing and crystallizing district (1010);
Be arranged on the mother liquor reflux inlet on oxidizing and crystallizing district (1010) tower body (101);
Be arranged on the circulating absorption solution outlet on oxidizing and crystallizing district (1010) air-distributor (1011) the below tower body (101);
Be arranged on the sulphur ammonium slurry outlet on oxidizing and crystallizing district (1010) air-distributor (1011) the below tower body (101);
A feature of the present invention is, the incoming interface that adds of sweetening agent ammonia is arranged on the desulphurization circulating pipeline, be not arranged on the tower body, be not arranged on the deamination circulation line 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 sulfurous gas, even be absorbed as main zone, reduce the ammonia loss by volatilization in the tail gas to greatest extent with ammonia.
Second feature of the present invention be, deamination district height H 1 is 1～10m, and better between 2～6m, the superficial velocity of waste gas by the deamination district is preferably between 2.0～3.5m/s between 1～5m/s, determines the diameter in deamination district in view of the above.
The height of desulfurization zone is 5～20m, and better between 8～15m, its diameter is identical with the deamination district.
The height in oxidizing and crystallizing district is preferably between 8～15m between 5～20m, and its diameter is 1～2 times of deamination district diameter.
The 3rd feature of the present invention is that deamination and desulfurization absorption liquid sparger comprise a house steward, and some arms that link to each other with house steward, with the nozzle that is connected with arm.The internal diameter size that house steward and Zhi see is that 1～5m/s determines according to the velocity of flow of absorption liquid in pipe, better determines according to 1.5～2.5m/s.
The 4th feature of the present invention be, 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 5～150mm, better between 20～80mm.The angle of the spray liquid of nozzle ejection is between 50～160 degree, better between 80～130 degree.The distribution density of nozzle number is that the basis is 0.3～5.0 nozzle/m with the cross-sectional area of corresponding zone
2, be 1～3 nozzle/m better
2
The 5th feature of the present invention be, desired deamination district, and perhaps the specific liquid rate of the absorption liquid of desulfurization zone based on the cross-sectional area of correspondence, is 5～300m
3/ m
2/ h, more preferably 10～200m
3/ m
2/ h is preferably 20～100m
3/ m
2/ h.The size of corresponding pump flow is determined on this basis.
The 6th feature of the present invention is to be arranged on gas, the liquid/gas separator of deamination absorption liquid sparger top, in order to separate droplets entrained in the tail gas.And this separator is that the fibre-reinforced sheet plastic of employing is that the corrugated cardboard sheet that material preparation becomes combines.Gauge of sheet is between 0.5～5mm, better between 1.0～3.0mm; The spacing of adjacent two corrugated cardboard sheets is 10～100mm, better between 20～50mm.The peak valley height of ripple is 50～500mm, more preferably 100～300mm; The width of the single ripple of ripple is 50～500mm, better at 100～300mm.
The 7th feature of the present invention be, is arranged on gas, liquid/gas separator wash-down water sparger up and down, and it is made up of wash-down water house steward, arm and nozzle.
The 8th feature of the present invention be, exhaust gas entrance is a rectangular opening, and the height of rectangular opening and the ratio of length are 0.2～0.8, and purpose is to reduce the total height of tower body as far as possible, reduces cost.
The 9th feature of the present invention is to be arranged on the waste gas sparger of desulfurization zone.
The waste gas sparger is a sieve plate, and its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 20～50%, and the bore dia of perforate is 10～100mm;
The waste gas sparger is a screen, and its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 20～50%, and the width in grizzly bar slit is 10～100mm, and length is 0.5～5.0m.
The of the present invention ten feature be, be arranged in the deamination district and desulfurization zone in reinforcement gas, liquid contact efficiency, promptly improve the reduction wall stream effect of deamination efficient and desulfuration efficiency and prevent the back-up ring of waste gas short circuit, the angle of back-up ring and tower wall 10～80 spend between.The length of back-up ring is between 0.1～3.0m.If back-up ring is an integral body not necessarily, can segmentation, the sectional hop count is between 2～20.
Description of drawings
Fig. 1 is the sulfur dioxide recovery device sketch of this invention.
The sulfurous gas absorption tower sketch that Fig. 2 comprises for the sulfur dioxide recovery device.
Embodiment
Referring to Fig. 1 and Fig. 2, method of the present invention comprises the steps:
Contain SO
2Waste gas, temperature is 100～200 ℃, at first deliver to the exhaust gas inlet 1013 on sulfurous gas absorption tower 1 by waste gas booster fan 2, after process waste gas sparger 109 is evenly distributed, upwards flow into desulfurization zone 108, with spray by desulfurization absorption liquid sparger 107, even also comprise the absorption liquid that contains ammonia that deamination absorption liquid sparger 105 sprays, counter current contact, absorb the sulfurous gas in the waste gas, generate ammonium sulphite, waste gas is absorbed the liquid Quench simultaneously, temperature is reduced between 50-60 ℃, and other pollutents in the waste gas also are absorbed; Waste gas continues upwards to flow, wherein can contain gaseous ammonia, the sulfurous gas that is not absorbed fully in addition, enter deamination district 106, with the absorption liquid that sprays by deamination absorption liquid sparger 105, counter current contact absorbs ammonia and sulfur dioxide gas in the waste gas, realizes the purpose that ammonia is deviate from and reclaimed.Behind desulfurization zone 108 and deamination district 106, the assimilated efficiency of the sulfurous gas in the waste gas can reach more than the 95-99%, and the ammonia content of wherein carrying secretly can be lower than 10mg/Nm
3Waste gas continues upwards to flow, through being arranged on gas, the liquid/gas separator 103 of deamination absorption liquid sparger 105 tops, remove droplets entrained after, by waste gas outlet 102, leave sulfurous gas absorption tower 1, through exhaust pass, the smoke stack emission that enters the downstream.
In order to obtain good assimilation effect, require the flow of desulfurization absorption liquid, perhaps the flow of deamination absorption liquid reaches 10-100m
3/ m
2The specific liquid rate of/h.
By the be absorbed absorption liquid that contains ammonium sulphite of sulfurous gas of desulfurization zone 108 and deamination district 106, wherein major part is an ammoniumsulphate soln, also contains the ammonium sulfate crystallization body, thereby is called the pulpous state absorption liquid.Absorption liquid directly falls into the oxidizing and crystallizing district that is positioned at 1 bottom, sulfurous gas absorption tower, and with the air of being sent into by oxidation air gas blower 3, after the contact of air-distributor 1011 bubblings, the ammonium sulphite in the absorption liquid is oxidized to ammonium sulfate; The concentration of ammonium sulfate surpass its corresponding solubleness to a certain degree after, ammonium sulfate can crystallization be separated out solid, obtains solid ammonium sulfate.Mass transfer for the promotes oxidn needs, and the mass transfer of crystallization needs, above air-distributor 1011, arranged agitator 1012, simultaneously in order to prevent that deposition of solids from luming on the floor on absorption tower, also arranged agitator 1012 below air-distributor 1011.
Go the absorption liquid in sulfurous gas absorption tower 1 desulfurization zone 108 and deamination district 106 to take out from the desulfurization absorption liquid and the outlet of deamination absorption liquid in the oxidizing and crystallizing district 1010 of 1 bottom, sulfurous gas absorption tower, pass through desulfuration recycle pump 5 respectively, with deamination recycle pump 4, deliver to corresponding desulfurization absorption liquid interface and deamination absorption liquid interface, enter corresponding desulfurization absorption liquid sparger 107 and deamination absorption liquid sparger 105 distribution sprays again.Especially, requirement of the present invention, desulfurization material ammonia add incoming interface, or claim ammonification mixing tank 6 to be arranged on the circulation line of desulfurization absorption liquid, can be in the inlet ductwork of desulfuration recycle pump 5, also can be on its export pipeline.
The solid ammonium sulfate slurries that form in the oxidizing and crystallizing district 1010 of 1 bottom, sulfurous gas absorption tower, a pump can be set separately to be extracted from the outlet of sulphur ammonium slurries, deliver to the sulphur ammonium and extract equipment 7, through concentrating, operations such as separation, drying, packing obtain the commodity thiamine fertilizer that can sell, remaining liquid is circulated back to oxidizing and crystallizing district 1010 recrystallize again.
In addition, the sulfurous gas absorption process is followed the Quench cooling of high-temp waste gas, needs consume water.Water of the present invention adds the implantation site and is arranged on gas, the liquid/gas separator wash-down water accumulator 8.Owing to the waste gas entrained liquids after the desulfurization enters gas, liquid/gas separator dehydration, be easy to adhere to sulphur ammonium crystal on the separator member, regularly flushing, otherwise separator obstruction, influence is operation normally.But because washing water quantity is bigger, and service discharge must satisfy the balance of water, and is generally less.After the wash-down water accumulator is set, can meet this requirement.
Embodiment 1
The fluidized-bed combustion boiler of a 440T/h uses the coal of sulphur content 1.5%, and flue-gas flow rate is 500,000 Nm
3/ hr, SO
2Content is 3200mg/Nm
3, the content of other pollutents is in the flue gas: dirt=80mg/Nm
3, SO
3=55mg/Nm
3, HCl=35mg/Nm
3, HF=20mg/Nm
3, NOx=100mg/Nm
3, flue-gas temperature is 120 ℃.
The raw material that sulfurous gas absorbs is 18% ammonia water mixture for the ammonia weight concentration.
The cat head central position on sulfurous gas absorption tower is provided with circular flue outlet, at the tower body internal upper part gas, liquid separating member is set; The wash-down water sparger that is connected with water inlet is set below gas, liquid separating member; The deamination circulating absorption solution sparger that is connected with the import of ammonia circulating absorption solution is set below the wash-down water sparger; Below deamination circulating absorption solution sparger, the deamination district is set; The desulphurization circulating absorption liquid sparger that is connected with the import of desulphurization circulating absorption liquid is set below the deamination district; Below desulphurization circulating absorption liquid sparger, desulfurization zone is set; At desulfurization zone smoke inlet is set; Absorption liquid overflow outlet is set on tower body; Below the overflow outlet, the oxidizing and crystallizing district is set; The circulating absorption solution outlet is set in bottom, oxidizing and crystallizing district, and connects the absorption liquid outlet, and connect the desulfuration recycle pump of the desulphurization circulating absorption liquid import on tower body top, with the deamination recycle pump that is connected the import of deamination circulating absorption solution; In bottom, oxidizing and crystallizing district the mother liquor reflux inlet is set; The air-distributor that is connected with gas inlet is set below the oxidizing and crystallizing district; On air-distributor top agitator is set; In the air-distributor bottom agitator is set; Sulphur ammonium slurry outlet is set in the air-distributor bottom; At relevant position the outlet of connection tower body circulating absorption solution, the desulphurization circulating pipe of desulfuration recycle pump and desulfurization absorption liquid sparger are set; At relevant position the outlet of connection tower body circulating absorption solution, the deamination circulation tube of deamination recycle pump and deamination absorption liquid sparger are set; On the desulphurization circulating pipe, be provided with the ammonia mixing tank.
In addition, the incoming interface that adds of sweetening agent ammonia is arranged on the desulphurization circulating pipeline, is not arranged on the tower body, also is not arranged on the deamination circulation line; Deamination district height H 1 is 5m, and flue gas is 3m/s by the superficial velocity in deamination district, determines the diameter in deamination district in view of the above; The height of desulfurization zone is 12m, and its diameter is identical with the deamination district; The height in oxidizing and crystallizing district is 9m, and its diameter is 1.6 times of deamination district diameter; Deamination and desulfurization absorption liquid sparger comprise a house steward, and some arms that link to each other with house steward, with the nozzle that is connected with arm.The internal diameter size of house steward and arm is that 2m/s determines according to the velocity of flow of absorption liquid in pipe.
Nozzle is a spiral nozzle, and the rotation number of turn of spiral is 4 circles.The spout internal diameter of spiral nozzle is 30mm.The angle of the spray liquid of nozzle ejection is 90 degree.The distribution density of nozzle number is based on the cross-sectional area of corresponding zone, preferred 2 the nozzle/m of present embodiment
2
The deamination district, the perhaps specific liquid rate of the absorption liquid of desulfurization zone, based on the cross-sectional area of correspondence, the preferred 30m of present embodiment
3/ m
2/ h.The size of corresponding pump flow is determined on this basis.
The gas, the liquid/gas separator that are arranged on deamination absorption liquid sparger top are used for separating the tail gas droplets entrained.It is that the corrugated cardboard sheet that material preparation becomes combines that this separator adopts glass fibre enhanced sheet plastic.Gauge of sheet is that the spacing of adjacent two corrugated cardboard sheets of 2mm is 30mm.The peak valley height of ripple is 200mm; The width of the single ripple of ripple is 200mm.
Being arranged on gas, liquid/gas separator two groups of wash-down water spargers up and down is made up of wash-down water house steward, arm and nozzle.
Smoke inlet is a rectangular opening, and the height of rectangular opening and the ratio of length are 0.32.The flue gas distributor that is arranged on desulfurization zone is a sieve plate, and its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 30%, and the bore dia of perforate is 20mm; Flue gas distributor is a screen, and then its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 40%, and the width in grizzly bar slit is 30mm, and length is 1m.In addition, be arranged in the deamination district and desulfurization zone in the angle of back-up ring and tower wall be 30 to spend.The length of back-up ring is 2m.Back-up ring is divided into 5 sections.
Through behind the scavenging tower, the purification efficiency of each pollutent is as follows:
SO
2＝97.8％，SO
3＝100％，HCl＝100％。HF=100%, NOx=22.5%, dirt=89%.
In the pulpous state solution that the oxidizing and crystallizing district is got rid of, solids content is 14.8%, behind over cure ammonium extraction equipment, is met the thiamine fertilizer product of national standard, and nitrogen content is 20.9, and water content is 0.4%, and throughput is 3.36 tons/hour.
Through behind the desulfurizing and purifying, the temperature of flue gas is 52.5 ℃.
A 300MW unit uses the coal of sulphur content 3.5%, and flue-gas flow rate is 1,200,000 Nm
3/ hr, SO
2Content is 9000mg/Nm
3, the content of other pollutents is in the flue gas: dirt=220mg/Nm
3, SO
3=105mg/Nm
3, HCl=35mg/Nm
3, HF=20mg/Nm
3, NOx=500mg/Nm
3, flue-gas temperature is 135 ℃.
The raw material that sulfurous gas absorbs is a liquefied ammonia.
The exhanst gas outlet on sulfurous gas absorption tower is arranged on the tower body of tower top near cat head, is rectangular opening; At the tower body internal upper part gas, liquid separating member are set; The wash-down water sparger that is connected with water inlet is set below gas, liquid separating member; The deamination circulating absorption solution sparger that is connected with the import of deamination circulating absorption solution is set below the wash-down water sparger; Below deamination circulating absorption solution sparger, the deamination district is set; The desulphurization circulating absorption liquid sparger that is connected with the import of desulphurization circulating absorption liquid is set below the deamination district; Below desulphurization circulating absorption liquid sparger, desulfurization zone is set; At desulfurization zone smoke inlet is set; Absorption liquid overflow outlet is set on tower body; Below the overflow outlet, the oxidizing and crystallizing district is set; The circulating absorption solution outlet is set in bottom, oxidizing and crystallizing district, and connects the absorption liquid outlet, and connect the desulfuration recycle pump of the desulphurization circulating absorption liquid import on tower body top, with the deamination recycle pump that is connected the import of deamination circulating absorption solution; In bottom, oxidizing and crystallizing district the mother liquor reflux inlet is set; The air-distributor that is connected with gas inlet is set below the oxidizing and crystallizing district; On air-distributor top agitator is set; In the air-distributor bottom agitator is set; Sulphur ammonium slurry outlet is set in the air-distributor bottom; At relevant position the outlet of connection tower body circulating absorption solution, the desulphurization circulating pipe of desulfuration recycle pump and desulfurization absorption liquid sparger are set; At relevant position the outlet of connection tower body circulating absorption solution, the deamination circulation tube of deamination recycle pump and deamination absorption liquid sparger are set; On the desulphurization circulating pipe, be provided with the ammonia mixing tank.
In addition, the incoming interface that adds of sweetening agent ammonia is arranged on the desulphurization circulating pipeline, is not arranged on the tower body, also is not arranged on the deamination circulation line; Deamination district height H 1 is 4.5m, and flue gas is 3.25m/s by the superficial velocity in deamination district, determines the diameter in deamination district in view of the above; The height of desulfurization zone is 11.5m, and its diameter is identical with the deamination district; The height in oxidizing and crystallizing district is 12.5m, and its diameter is 1.5 times of deamination district diameter; Deamination and desulfurization absorption liquid sparger comprise a house steward, and some arms that link to each other with house steward, with the nozzle that is connected with arm.The internal diameter size of house steward and arm is determined according to 2.5m/s according to the velocity of flow of absorption liquid in pipe.
Nozzle is a spiral nozzle, and the rotation number of turn of spiral is chosen to be 3 circles.The spout internal diameter of spiral nozzle is 45mm.The angle of the spray liquid of nozzle ejection is 120 degree.The distribution density of nozzle number is based on the cross-sectional area of corresponding zone, preferred 1.5 the nozzle/m of present embodiment
2
The deamination district, the perhaps specific liquid rate of the absorption liquid of desulfurization zone, based on the cross-sectional area of correspondence, the preferred 40m of present embodiment
3/ m
2/ h.The size of corresponding pump flow is determined on this basis.
The gas, the liquid/gas separator that are arranged on deamination absorption liquid sparger top are used for separating the tail gas droplets entrained.It is that the corrugated cardboard sheet that material preparation becomes combines that this separator adopts fibre-reinforced acrylic plastering thin plate.Gauge of sheet is 3.0mm; The spacing of adjacent two corrugated cardboard sheets is 28mm.The peak valley height of ripple is 190mm; The width of the single ripple of ripple is 190mm.
Being arranged on gas, liquid/gas separator two groups of wash-down water spargers up and down is made up of wash-down water house steward, arm and nozzle.
Smoke inlet is a rectangular opening, and the height of rectangular opening and the ratio of length are 0.28.The flue gas distributor that is arranged on desulfurization zone is a sieve plate, and its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 35%, and the bore dia of perforate is 18mm; Flue gas distributor is a screen, and then its percentage of open area (cross-sectional area of the total area/tower body of perforate) is 30%, and the width in grizzly bar slit is 28mm, and length is 0.8m.In addition, be arranged in the deamination district and desulfurization zone in the angle of back-up ring and tower wall be 28 to spend.The length of back-up ring is 2.8m.Back-up ring is divided into 7 sections.
Through behind the scavenging tower, the purification efficiency of each pollutent is as follows:
SO
2＝98.8％，SO
3＝100％，HCl＝100％。HF=100%, NOx=28.5%, dirt=91%.
In the pulpous state solution that the oxidizing and crystallizing section is got rid of, solids content is 15.8%, behind over cure ammonium extraction equipment, is met the thiamine fertilizer product of national standard, and nitrogen content is 20.85, and water content is 0.42%, and throughput is 22.72 tons/hour.
Through behind the desulfurizing and purifying, the temperature of flue gas is 53.5 ℃.
Claims (10)
1. production equipment by waste gas sulfate ammonium, it comprises sulfurous gas absorption tower (1), said sulfurous gas absorption tower (1) comprises three functional modules: deamination district (106), desulfurization zone (108) and oxidizing and crystallizing district (1010) is characterized in that
The deamination district is positioned between deamination absorption liquid sparger and the desulfurization absorption liquid sparger;
Desulfurization zone is between desulfurization absorption liquid sparger and overflow outlet;
The oxidizing and crystallizing district is positioned between overflow outlet and the tower base plate.
2. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises the waste gas booster fan (2) that is connected with sulfurous gas absorption tower (1).
3. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises the oxidation air gas blower (3) that is connected with sulfurous gas absorption tower (1).
4. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises the deamination absorption liquid recycle pump (4) that is connected with sulfurous gas absorption tower (1).
5. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises the desulfurization absorption liquid recycle pump (5) that is connected with sulfurous gas absorption tower (1).
6. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises and advances ammonia mixing tank (6) on the absorption liquid circulation line that is connected with described desulfurization absorption liquid recycle pump (5).
7. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment comprises that also the sulphur ammonium that is connected with sulfurous gas absorption tower (1) extracts equipment (7).
8. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described production equipment also comprises gas, the liquid/gas separator wash-down water accumulator (8) that is connected with sulfurous gas absorption tower (1).
9. the production equipment by waste gas sulfate ammonium according to claim 1 is characterized in that, described sulfurous gas absorption tower (1) also comprises:
Be arranged on the purifying exhaust air outlet (102) of cat head;
Be arranged on gas, the liquid separating member (103) of tower body (101) internal upper part;
Be arranged on the wash-down water sparger (104) that is connected with water inlet in gas, the liquid separating member (103);
Be arranged on the deamination circulating absorption solution sparger (105) that is connected with the import of deamination circulating absorption solution of wash-down water sparger (104) below;
Be arranged on the desulphurization circulating absorption liquid sparger (107) that is connected with the import of desulphurization circulating absorption liquid of below, deamination district (106);
Be arranged on the exhaust gas entrance (1013) of desulfurization zone (108);
Be arranged on the oxidizing and crystallizing district (1010) of exhaust gas entrance (1013) below;
Be arranged on the air-distributor that is connected with gas inlet (1011) in oxidizing and crystallizing district (1010);
Be arranged on the agitator (1012) of air-distributor (1011) top or the bottom of oxidizing and crystallizing district (1010);
Be arranged on the mother liquor reflux inlet on oxidizing and crystallizing district (1010) tower body (101);
Be arranged on the circulating absorption solution outlet on oxidizing and crystallizing district (1010) air-distributor (1011) the below tower body (101).
10. the production equipment by waste gas sulfate ammonium according to claim 9, it is characterized in that described sulfurous gas absorption tower (1) also comprises the sulphur ammonium slurry outlet that is arranged on oxidizing and crystallizing district (1010) air-distributor (1011) the below tower body (101).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101302189A CN101100301A (en) | 2007-07-16 | 2007-07-16 | Device for producing ammonium sulfate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101302189A CN101100301A (en) | 2007-07-16 | 2007-07-16 | Device for producing ammonium sulfate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101100301A true CN101100301A (en) | 2008-01-09 |
Family
ID=39034785
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007101302189A Pending CN101100301A (en) | 2007-07-16 | 2007-07-16 | Device for producing ammonium sulfate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101100301A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110479077A (en) * | 2019-09-17 | 2019-11-22 | 上海蓝科石化环保科技股份有限公司 | A kind of ammonia process of desulfurization oxidation unit and method |
| CN111573695A (en) * | 2020-04-09 | 2020-08-25 | 浙江省天正设计工程有限公司 | Recycling treatment process for high-concentration organic wastewater containing phosphorus and sulfur |
| CN110479077B (en) * | 2019-09-17 | 2024-05-03 | 上海蓝科石化环保科技股份有限公司 | Ammonia desulfurization and oxidation device and method |
-
2007
- 2007-07-16 CN CNA2007101302189A patent/CN101100301A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110479077A (en) * | 2019-09-17 | 2019-11-22 | 上海蓝科石化环保科技股份有限公司 | A kind of ammonia process of desulfurization oxidation unit and method |
| CN110479077B (en) * | 2019-09-17 | 2024-05-03 | 上海蓝科石化环保科技股份有限公司 | Ammonia desulfurization and oxidation device and method |
| CN111573695A (en) * | 2020-04-09 | 2020-08-25 | 浙江省天正设计工程有限公司 | Recycling treatment process for high-concentration organic wastewater containing phosphorus and sulfur |
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Open date: 20080109 |