CN102527210A - Sintering flue gas ammonia desulfurization system and process - Google Patents
Sintering flue gas ammonia desulfurization system and process Download PDFInfo
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- CN102527210A CN102527210A CN201010614694XA CN201010614694A CN102527210A CN 102527210 A CN102527210 A CN 102527210A CN 201010614694X A CN201010614694X A CN 201010614694XA CN 201010614694 A CN201010614694 A CN 201010614694A CN 102527210 A CN102527210 A CN 102527210A
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Abstract
The invention relates to a sintering flue gas ammonia desulfurization system and a sintering flue gas ammonia desulfurization process. The sintering flue gas ammonia desulfurization system comprises an ammonia supply system, an absorption system, a filtration system and an oxidation system, wherein the ammonia supply system is connected with the absorption system which is connected with the filtration system; and the filtration system is connected with the oxidation system. The sintering flue gas ammonia desulfurization system can effectively remove sulfur dioxide from flue gas, and reduces the escape degree of ammonia; a generated byproduct ammonium sulfite is filtered, is subjected to impurity removal and then is subjected to low-concentration normal-pressure oxidation, so that the conversion rate of ammonia sulfate is guaranteed, and a qualified raw material solution is provided for a next-stage ammonia sulfate preparation system; the sintering flue gas ammonia desulfurization system has a reasonable structure, ensures that the flue gas reaches standard to discharge and reduces secondary pollution caused by escaped ammonia; and the qualified raw material solution is provided for the next-stage ammonia sulfate preparation system through the pretreatment process of the byproduct of filtering first and then oxidizing, so that the quality of a byproduct ammonia sulfate is ensured.
Description
Technical field
The present invention relates to a kind of desulphurization system and technology, relate in particular to a kind of sintering flue gas ammonia method desulfurizing system and technology, belong to the flue gas desulfurization field.
Background technology
Sulfur dioxide in the sinter fume is one of main root of atmosphere pollution, and the ammonia process of desulfurization utilizes absorption liquid and flue gas to react, and is the better method that sulfur dioxide in flue gas is administered that adopts at present.In the present ammonia process commonly used, the oxidation of ammonium sulfite is carried out in desulfurizing tower usually, and oxidation efficiency is low, and specific air consumption is big; Escape problem to ammonia in the desulfurizing tower still can not adopt a kind of effective method to go to solve; Processing mode to dust in the sinter fume is improper, has influenced the color and luster and the quality of ammonium sulfate.
Chinese patent CN 101053760A discloses a kind of sintering flue gas ammonia method desulfurizing system; This system is because adopt the low temperature ammonia process to carry out desulfurization; The position of mending ammonia biases toward the top of whole desulfurizing tower in spraying layer, cause ammonia also not have complete reaction easily; Promptly escape, so the loss phenomenon of ammonia is more serious along with the flue gas volatilization; And the total system employing is to carry out sulfite oxidation, the flow process that again ammonium sulfate is concentrated, filters earlier.Contain dust in the ammonium sulfite solution, can reduce oxidation efficiency, the sulphur ammonium transforms not exclusively, influences product gas purity.Ammonium sulfate has absorbed the part sulfur dioxide in the flue gas and solution acidic is strengthened in concentration process, causes the aggravation to back level equipment corrosion; Most of dust in the flue gas can enter in the solution and form colloidal state with ammonium sulfate simultaneously, and because ammonium sulfate concentration becomes big, makes relatively difficulty of filter operation; The filter residue that filters does not have processing scheme, not only can form new pollution, and influence the overall productivity of ammonium sulfate.
Summary of the invention
The present invention is directed to the above-mentioned deficiency that existing sintering flue gas ammonia method desulfurizing system exists, a kind of sintering flue gas ammonia method desulfurizing system and technology are provided.
The technical scheme that the present invention solves the problems of the technologies described above is following: a kind of sintering flue gas ammonia method desulfurizing system comprises confession ammonia system, absorption system, filtration system and oxidative system; Said confession ammonia system links to each other with absorption system; Said absorption system links to each other with filtration system, and said filtration system links to each other with oxidative system; Said confession ammonia system comprises the liquefied ammonia feeding mechanism; The ammonia absorber that links to each other with said liquefied ammonia feeding mechanism; The concentrated ammonia liquor storage tank that links to each other with said ammonia absorber, the aqua ammonia pump that links to each other with said concentrated ammonia liquor storage tank, the pipe-line mixer that links to each other with said aqua ammonia pump; The ammoniacal liquor surge tank that links to each other with said pipe-line mixer, and the confession ammonia pump that links to each other with said ammoniacal liquor surge tank; Said absorption system comprises reaction tower, and what link to each other with said reaction tower is connected flue, and is connected the scrubbing tower that flue links to each other with said, and said reaction tower links to each other with the confession ammonia pump; Said filtration system comprises the turbid liquid pump that links to each other with said scrubbing tower; The turbid liquid centrifuge that links to each other with said turbid liquid pump, the filtration pans that link to each other with said turbid liquid centrifuge and mistake filter residue flow container, the clear liquid pump that links to each other with said filtration pans; The accurate filter that links to each other with said clear liquid pump; Cross the press filtration pump that the filter residue flow container links to each other with said, and the filter press that links to each other with said press filtration pump, the said filter residue flow container of crossing links to each other with accurate filter; Said oxidative system comprises the oxidizing tower that links to each other with said accurate filter, and the oxidation fan that links to each other with said oxidizing tower.
The invention has the beneficial effects as follows: sintering flue gas ammonia method desulfurizing system of the present invention can not only be removed sulfur in smoke effectively; And reduced the escape degree of ammonia; The accessory substance ammonium sulfite that is generated carries out the low concentration atmospheric pressure oxidation through behind the filtering and impurity removing; Ensured the conversion ratio of ammonium sulfate, for back grade ammonium sulfate preparation system provides qualified material solution; Sintering flue gas ammonia method desulfurizing system of the present invention rational in infrastructure; Make the flue gas qualified discharge and reduced the secondary pollution that escape ammonia produces; Through filtering the accessory substance processing procedure in early stage of rear oxidation earlier; For back grade ammonium sulfate preparation system provides qualified material liquid, guaranteed the quality of producing ammonium sulfate byproduct.
On the basis of technique scheme, the present invention can also do following improvement.
Further, the top of said reaction tower is connected with smoke inlet, and said reaction tower is positioned at the top that connects flue and comprises tubular reactor, and said tubular reactor comprises the ammonia spray device, and said tubular reactor links to each other with the confession ammonia pump; Said reaction tower is positioned at the bottom that connects flue and comprises the washing liquid bath, said washing liquid bath through dividing plate be connected flue and separate.
Further, the top of said scrubbing tower is connected with exhanst gas outlet, and said scrubbing tower is positioned at the top that connects flue and is divided into the dehydrating demisting section from top to bottom, washes ammonia section and washing section; Said scrubbing tower is positioned at the bottom that connects flue and comprises the slurries memory block.
Further, said dehydrating demisting section with wash the ammonia section and be separated by first dividing plate, said first dividing plate has a plurality of first gas caps towards an end of dehydrating demisting section; Saidly wash the ammonia section and washing section is separated by second partition, said second partition has a plurality of second gas caps towards an end of washing the ammonia section.
Further, said dehydrating demisting section comprises at least one demister; The said ammonia section of washing comprises one deck cleaning solution spray equipment at least; Said washing section comprises one deck slurries spray equipment at least, and the air ducting that is positioned at slurries spray equipment below, said air ducting with is connected the setting of flue correspondence.
Further, said first dividing plate links to each other with the washing liquid bath through pipeline respectively with second partition.
Further, said washing liquid bath links to each other with slurry tank with the cleaning solution spray equipment respectively through detergent circulator, and said slurries memory block links to each other with the slurries spray equipment through slurry circulating pump.
Further; Said oxidative system also comprises aeration circulating pump and sulphur ammonium liquid storage tank; The bottom of said oxidizing tower links to each other through the top of aeration circulating pump and oxidizing tower, and simultaneously, the bottom of said sulphur ammonium liquid storage tank and oxidizing tower links to each other; The inwall of said oxidizing tower is provided with heat exchanger, and said heat exchanger radially is circle distribution along oxidizing tower.
The present invention also provides a kind of technical scheme that solves the problems of the technologies described above following: a kind of sintering flue gas ammonia method desulfurizing technology may further comprise the steps:
A. to change into concentration be 15%～25% concentrated ammonia liquor and put into the concentrated ammonia liquor storage tank and store through ammonia absorber with the liquefied ammonia in the liquefied ammonia feeding mechanism;
B. the concentrated ammonia liquor in the concentrated ammonia liquor storage tank is extracted out and is transported to through aqua ammonia pump in the pipe-line mixer and is delivered to the ammoniacal liquor surge tank after fresh water (FW) mixes and carries out buffer memory;
C. the mixed liquor with concentrated ammonia liquor and fresh water (FW) is transported in the reaction tower through supplying ammonia pump; Itself and the sinter fume that enters in the reaction tower are reacted and heat exchange; Temperature is between 55 ℃～150 ℃ in the reaction tower; Flue gas is no more than 2 seconds at the reaction dwell time in the tower, and the inwall of tubular reactor has corrosion resistance;
D. reacted sinter fume gets in the scrubbing tower through connecting flue; After get into washing section in the scrubbing tower successively, washing ammonia section and dehydrating demisting section; Discharge from scrubber overhead; Washing section is used for spraying the ammonium sulfite particle and the dust of the sinter fume behind the absorption reaction, and the slurries behind the spray are stored in scrubbing tower and are positioned at the slurries memory block, bottom that connects flue, and washing section and the liquid-gas ratio of washing the ammonia section are controlled between 1～10;
The slurries that e. will contain ammonium sulfite are delivered to turbid liquid centrifuge through turbid liquid pump to carry out one-level and filters and obtain filtrating and filter residue, and filtrating is delivered to the filtration pans, and filter residue was delivered to the filter residue flow container;
F. will filtrate and carry out cascade filtration and obtain clear liquid and filter residue from filtering pans and extract out and be delivered to accurate filter through clear liquid pump; And clear liquid is delivered to carries out the aeration oxidation in the oxidizing tower; Backwashing water is delivered to accurate filter to be made the filter residue backwash come out to form slag liquid to be delivered to the filter residue flow container; Through the press filtration pump slag liquid is delivered to filter press and carries out press filtration, fluid temperature is no more than 60 ℃ in the oxidizing tower, uses the atmosphere through dedusting to carry out oxidation in the oxidizing tower; Keep coefficient of excess air between 1.25～2, guarantee that liquid is not less than 6 hours at the oxidation dwell time in the tower.
Further; The bottom of said oxidizing tower links to each other through the top of aeration circulating pump and oxidizing tower; The clear liquid that is delivered in the oxidizing tower is carried out circulated sprinkling from the top that is delivered to oxidizing tower after the oxidizing tower bottom is extracted; Simultaneously, the bottom of said oxidizing tower links to each other with sulphur ammonium liquid storage tank, the clear liquid after the oxidation is delivered to sulphur ammonium liquid storage tank deposits.
Description of drawings
Fig. 1 is the structural representation of sintering flue gas ammonia method desulfurizing system of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing principle of the present invention and characteristic are described, institute gives an actual example and only is used to explain the present invention, is not to be used to limit scope of the present invention.Fresh water (FW) among Fig. 1 is meant the deionized water of handling through water softening device.Flushing water is meant the manufacture water.Backwash water is meant the industry water through multistage filtering, and the impurity particle diameter is no more than 0.3 micron in the water.Recirculated water is meant that industry goes up in order rationally to use water resource, utilizes the bigger characteristics of water specific heat as the heating agent carrier, after cold water removes to absorb heat and heats up into hot water, again hot water is become cold water through the cooling means and recycles.
As shown in Figure 1, the liquefied ammonia feeding mechanism is that the concentrated ammonia liquor that external liquefied ammonia tank vehicle transforms written treaty about 20% through ammonia absorber 1 is placed on storage in the concentrated ammonia liquor storage tank 3.Get into ammoniacal liquor surge tank 5 buffer memorys after being mixed into the concentration of instructions for use with fresh water (FW) when concentrated ammonia liquor is extracted out through pipe-line mixer 6 by aqua ammonia pump, then with supplying ammonia pump 4 to deliver to interior ammonia spray device 7 atomized spray of tubular reactor 8 of reaction tower 10.Sinter fume gets into from the smoke inlet 9 on reaction tower 10 tops, in tubular reactor 8, and the SO in the flue gas
2Ammoniacal liquor after the atomizing of spraying with ammonia spray device 7 reacts and heat exchange, accomplishes desulfurization, denitration.Flue gas after the desulfurization enters into scrubbing tower 11 through the connection flue 21 between the double tower.The reaction tower lower space is washing liquid bath 22, with dividing plate be connected flue and separate.
Scrubbing tower 11 is the multistage washing tower, and flue gas gets into through connecting flue 21, through air ducting 20 upwards stream through washing section 18, wash ammonia section 16, dehydrating demisting section 13 after, from exhanst gas outlet 12 dischargings on scrubbing tower 11 tops.The space that connects flue 21 inlet scrubbing tower bottoms is the slurries memory block, and the storage loop slurry uses.Scrubbing tower 11 from top to bottom by gas cap 14 and dividing plate 15 be separated into dehydrating demisting section 13, wash ammonia section 16,18 3 functional areas of washing section, be used for removing the dirt in water smoke, escape ammonia, sulphur ammonium particle and the flue gas respectively.The effect of dividing plate 15 is that flushing water and cleaning solution are back to washing liquid bath 22, and gas cap 14 plays and ventilates and the evenly effect of distribution flue gas.Wash ammonium, wash the flue gas that the ammonia section captures behind the escape ammonia and after dehydrating demisting section 13 is removed fine drop by demister, enter atmosphere through the washing section dedusting.With flushing water demister is regularly cleaned.Wash the cleaning solution of more than one deck spray equipment 17 is arranged in the ammonia section 16.Cleaning solution spray equipment 17 is formed the functional areas that a washing removes escape ammonia with washing liquid bath 22 and cleaning circulation pump 23.After cleaning solution concentration reached finite concentration, the part cleaning solution was transported to the scrubbing tower bottom through cleaning circulation pump 23 to the lateral of the trunk line of spray equipment 17, as the additional liquid of loop slurry.Multilayer slurries spray equipment 19 is arranged in the washing section 18; Slurries in the slurries memory block extract through slurry circulating pump 24; Be delivered to slurries spray equipment 19 through piping and carry out atomizing spray, desulfurization product ammonium sulfite particle and dust in the slurries absorption and washing flue gas that sprays.After ammonium sulfite concentration in the slurries reaches the technological requirement index, deliver to the separation that filtration system is carried out dirt mud through turbid liquid pump extraction.Said dehydrating demisting section 13 is according to process condition adjustment spray washing intensity and frequency, and said spray flux of washing ammonia section 16 and washing section 18 is reasonably regulated according to technological requirement.
Filtration system adopts double-stage filtering, and ammonium sulfate solution is delivered to turbid liquid centrifuge 36 with turbid liquid pump 25 and carried out the one-level filtration, and filtrating advances to filter pans 35, and filter residue removed filter residue flow container 26.Clear liquid pump 34 is extracted the one-level filtered fluid out from filter pans 35, delivers to accurate filter 33 and carries out cascade filtration.The clear liquid that comes out from accurate filter is delivered to oxidizing tower 31 and is carried out the aeration oxidation, utilizes the backwash water backwash to wash the filter residue that comes from accurate filter and enters into filter residue flow container 26.Press filtration pump 27 will be crossed slag liquid in the filter residue flow container 26 and deliver to filter press 28 and carry out press filtration, and filtrating is returned the filtration pans, and filter cake is delivered to the stock ground.
After the clear liquid that comes out from accurate filter 33 got into oxidizing tower 31, oxidized blower fan 29 was sent into the air oxidation of oxidizing tower, in order to reach higher oxidation efficiency, with aeration circulating pump 30 from the oxidizing tower bottom extraction solution deliver to oxidizing tower top and carry out circulated sprinkling.Oxidizing tower is built-in with recuperator, said heat exchanger be arranged on the inwall of oxidizing tower and along oxidizing tower radially be circle distribution, regulate circulating water flow so that oxidizing temperature is controlled under the rational condition.Well-oxygenated ammonium sulfate is delivered to sulphur ammonium liquid storage tank 32 through pipeline and is deposited, as the material liquid of sulphur ammonium preparation system.
Sintering flue gas ammonia method desulfurizing system of the present invention is if adopting ammoniacal liquor is desulfurizing agent, and then ammonia absorber 1 can omit with aqua ammonia pump 2, and tubular reactor 8 can be that single tube also can be the multitube combination, and washing liquid bath 22 can be opened to set up and become independent equipment with reaction tower in 10 minutes.
Sintering flue gas ammonia method desulfurizing process using desulphurization reaction of the present invention, the flow process of washing ammonium deamination, filtering and impurity removing, the clean ammonium of oxidation; Make technology science, reasonable more; Adopt reaction tower to separate outfit, help the desulfurization demand of actual use and adaptation large scale sintering equipment with scrubbing tower.
Adopt the multi-layer classification spray washing in the scrubbing tower in the sintering flue gas ammonia method desulfurizing system of the present invention, absorbed the measure of escape ammonia, reduced the secondary pollution problem that escape ammonia causes; To sinter fume dust characteristics, the adjustable multistage filtering device of concentration is set, effectively remove metallic dust and recycle and reuse; Adopt the efficient oxidation tower, improve the conversion ratio of ammonium salt, reduce superfluous air quantity, energy efficient; The forced oxidation section, the mode of employing gas-liquid counter current and mass transfer tower tray efficiently come further accelerating oxidation effect, make the conversion ratio of ammonium sulfite remain on higher level; Adopt ammonia absorber rapidly liquefied ammonia to be changed into concentrated ammonia liquor and deposit, avoid potential safety hazard that the liquefied ammonia storage brings and too much place to take, use if metallurgical integrated complex has self-produced ammoniacal liquor directly to receive with the concentrated ammonia liquor storage tank, ammonia absorber 1 and aqua ammonia pump 2 can omit.
The above is merely preferred embodiment of the present invention, and is in order to restriction the present invention, not all within spirit of the present invention and principle, any modification of being done, is equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. sintering flue gas ammonia method desulfurizing system; It is characterized in that comprise supplying ammonia system, absorption system, filtration system and oxidative system, said confession ammonia system links to each other with absorption system; Said absorption system links to each other with filtration system, and said filtration system links to each other with oxidative system; Said confession ammonia system comprises the liquefied ammonia feeding mechanism; The ammonia absorber that links to each other with said liquefied ammonia feeding mechanism; The concentrated ammonia liquor storage tank that links to each other with said ammonia absorber, the aqua ammonia pump that links to each other with said concentrated ammonia liquor storage tank, the pipe-line mixer that links to each other with said aqua ammonia pump; The ammoniacal liquor surge tank that links to each other with said pipe-line mixer, and the confession ammonia pump that links to each other with said ammoniacal liquor surge tank; Said absorption system comprises reaction tower, and what link to each other with said reaction tower is connected flue, and is connected the scrubbing tower that flue links to each other with said, and said reaction tower links to each other with the confession ammonia pump; Said filtration system comprises the turbid liquid pump that links to each other with said scrubbing tower; The turbid liquid centrifuge that links to each other with said turbid liquid pump, the filtration pans that link to each other with said turbid liquid centrifuge and mistake filter residue flow container, the clear liquid pump that links to each other with said filtration pans; The accurate filter that links to each other with said clear liquid pump; Cross the press filtration pump that the filter residue flow container links to each other with said, and the filter press that links to each other with said press filtration pump, the said filter residue flow container of crossing links to each other with accurate filter; Said oxidative system comprises the oxidizing tower that links to each other with said accurate filter, and the oxidation fan that links to each other with said oxidizing tower.
2. sintering flue gas ammonia method desulfurizing system according to claim 1; It is characterized in that; The top of said reaction tower is connected with smoke inlet; Said reaction tower is positioned at the top that connects flue and comprises tubular reactor, and said tubular reactor comprises the ammonia spray device, and said tubular reactor links to each other with the confession ammonia pump; Said reaction tower is positioned at the bottom that connects flue and comprises the washing liquid bath, said washing liquid bath through dividing plate be connected flue and separate.
3. sintering flue gas ammonia method desulfurizing system according to claim 2 is characterized in that the top of said scrubbing tower is connected with exhanst gas outlet, and said scrubbing tower is positioned at the top that connects flue and is divided into the dehydrating demisting section from top to bottom, washes ammonia section and washing section; Said scrubbing tower is positioned at the bottom that connects flue and comprises the slurries memory block.
4. sintering flue gas ammonia method desulfurizing system according to claim 3 is characterized in that, said dehydrating demisting section with wash the ammonia section and be separated by first dividing plate, said first dividing plate has a plurality of first gas caps towards an end of dehydrating demisting section; Saidly wash the ammonia section and washing section is separated by second partition, said second partition has a plurality of second gas caps towards an end of washing the ammonia section.
5. according to claim 3 or 4 described sintering flue gas ammonia method desulfurizing systems, it is characterized in that said dehydrating demisting section comprises at least one demister; The said ammonia section of washing comprises one deck cleaning solution spray equipment at least; Said washing section comprises one deck slurries spray equipment at least, and the air ducting that is positioned at slurries spray equipment below, said air ducting with is connected the setting of flue correspondence.
6. sintering flue gas ammonia method desulfurizing system according to claim 4 is characterized in that, said first dividing plate links to each other with the washing liquid bath through pipeline respectively with second partition.
7. sintering flue gas ammonia method desulfurizing system according to claim 5; It is characterized in that; Said washing liquid bath links to each other with slurry tank with the cleaning solution spray equipment respectively through detergent circulator, and said slurries memory block links to each other with the slurries spray equipment through slurry circulating pump.
8. sintering flue gas ammonia method desulfurizing system according to claim 1; It is characterized in that said oxidative system also comprises aeration circulating pump and sulphur ammonium liquid storage tank, the bottom of said oxidizing tower links to each other through the top of aeration circulating pump and oxidizing tower; Simultaneously; The bottom of said sulphur ammonium liquid storage tank and oxidizing tower links to each other, and the inwall of said oxidizing tower is provided with heat exchanger, and said heat exchanger radially is circle distribution along oxidizing tower.
9. a sintering flue gas ammonia method desulfurizing technology is characterized in that, may further comprise the steps:
A. to change into concentration be 15%～25% concentrated ammonia liquor and put into the concentrated ammonia liquor storage tank and store through ammonia absorber with the liquefied ammonia in the liquefied ammonia feeding mechanism;
B. the concentrated ammonia liquor in the concentrated ammonia liquor storage tank is extracted out and is transported to through aqua ammonia pump in the pipe-line mixer and is delivered to the ammoniacal liquor surge tank after fresh water (FW) mixes and carries out buffer memory;
C. the mixed liquor with concentrated ammonia liquor and fresh water (FW) is transported in the reaction tower through supplying ammonia pump; Itself and the sinter fume that enters in the reaction tower are reacted and heat exchange; Temperature is between 55 ℃～150 ℃ in the reaction tower; Flue gas is no more than 2 seconds at the reaction dwell time in the tower, and the inwall of tubular reactor has corrosion resistance;
D. reacted sinter fume gets in the scrubbing tower through connecting flue; After getting into washing section in the scrubbing tower successively, washing ammonia section and dehydrating demisting section; Discharge from scrubber overhead; Washing section is used for spraying the ammonium sulfite particle and the dust of the sinter fume behind the absorption reaction, and the slurries behind the spray are stored in scrubbing tower and are positioned at the slurries memory block, bottom that connects flue, and washing section and the liquid-gas ratio of washing the ammonia section are controlled between 1～10;
The slurries that e. will contain ammonium sulfite are delivered to turbid liquid centrifuge through turbid liquid pump to carry out one-level and filters and obtain filtrating and filter residue, and filtrating is delivered to the filtration pans, and filter residue was delivered to the filter residue flow container;
F. will filtrate and carry out cascade filtration and obtain clear liquid and filter residue from filtering pans and extract out and be delivered to accurate filter through clear liquid pump; And clear liquid is delivered to carries out the aeration oxidation in the oxidizing tower; Backwashing water is delivered to accurate filter to be made the filter residue backwash come out to form slag liquid to be delivered to the filter residue flow container; Through the press filtration pump slag liquid is delivered to filter press and carries out press filtration, fluid temperature is no more than 60 ℃ in the oxidizing tower, uses the atmosphere through dedusting to carry out oxidation in the oxidizing tower; Keep coefficient of excess air between 1.25～2, guarantee that liquid is not less than 6 hours at the oxidation dwell time in the tower.
10. sintering flue gas ammonia method desulfurizing technology according to claim 9; It is characterized in that; The bottom of said oxidizing tower links to each other through the top of aeration circulating pump and oxidizing tower, carries out circulated sprinkling with being delivered to the top that clear liquid in the oxidizing tower is delivered to oxidizing tower after the extraction of oxidizing tower bottom, simultaneously; The bottom of said oxidizing tower links to each other with sulphur ammonium liquid storage tank, the clear liquid after the oxidation is delivered to sulphur ammonium liquid storage tank deposits.
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| CN104147913A (en) * | 2013-09-13 | 2014-11-19 | 上海大学 | Two-phase ammonifying method of wet ammonia desulfurization process |
| CN104147913B (en) * | 2013-09-13 | 2016-04-27 | 上海大学 | A kind of two-phase of wet ammonia process desulfurizing technology adds ammonia process |
| CN103752117A (en) * | 2014-01-23 | 2014-04-30 | 上海龙净环保科技工程有限公司 | Smoke-gas treatment system and method of integrated desulfuration and PM2.5 (Fine Particulate Matter) desorption by adopting ammonia process |
| CN103752117B (en) * | 2014-01-23 | 2016-03-23 | 上海龙净环保科技工程有限公司 | A kind of ammonia process integrated desulfurizing, remove the smoke gas treatment system and method for PM2.5 |
| CN103820171A (en) * | 2014-03-12 | 2014-05-28 | 邯郸市裕泰燃气有限公司 | Coal gas desulfurization device |
| CN103820171B (en) * | 2014-03-12 | 2016-03-16 | 邯郸市裕泰燃气有限公司 | Gas desulfurizer |
| CN103977693A (en) * | 2014-06-04 | 2014-08-13 | 长沙高必拓脱硫工程有限公司 | Pneumatic emulsion ammonium carbonate desulfurization system and technological process thereof |
| CN103977693B (en) * | 2014-06-04 | 2016-03-02 | 长沙高必拓脱硫工程有限公司 | A kind of Pneumatic emulsifying carbon ammonium desulphurization system and technological process thereof |
| CN109432995A (en) * | 2018-12-14 | 2019-03-08 | 四川金象赛瑞化工股份有限公司 | The processing method and processing unit of chemical industry tail gas |
| CN115178066A (en) * | 2022-08-24 | 2022-10-14 | 山东高瑞化工有限公司 | Comprehensive treatment system and treatment process for pyrazole inorganic waste gas |
| CN115178066B (en) * | 2022-08-24 | 2023-08-22 | 山东高瑞化工有限公司 | Comprehensive treatment system and treatment process for pyrazole inorganic waste gas |
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