CN102527210B - Sintering flue gas ammonia desulfurization system and process - Google Patents

Sintering flue gas ammonia desulfurization system and process Download PDF

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Publication number
CN102527210B
CN102527210B CN201010614694.XA CN201010614694A CN102527210B CN 102527210 B CN102527210 B CN 102527210B CN 201010614694 A CN201010614694 A CN 201010614694A CN 102527210 B CN102527210 B CN 102527210B
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ammonia
tower
flue gas
pump
washing
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CN201010614694.XA
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Chinese (zh)
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CN102527210A (en
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赵森林
冀留庆
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中钢集团工程设计研究院有限公司
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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

A kind of sintering flue gas ammonia method desulfurizing system and technique

Technical field

The present invention relates to a kind of desulphurization system and technique, particularly relate to a kind of sintering flue gas ammonia method desulfurizing system and technique, belong to flue gas desulfurization field.

Background technology

Sulfur dioxide in sinter fume is one of main contributor of atmosphere pollution, and the ammonia process of desulfurization utilizes absorbing liquid and flue gas to react, and is the better method administered sulfur dioxide in flue gas adopted at present.In current conventional ammonia process, the oxidation of ammonium sulfite is carried out usually in desulfurizing tower, and oxidation efficiency is low, and specific air consumption is large; A kind of effective method still can not be adopted to go to solve to the escape problem of ammonia in desulfurizing tower; Improper to the processing mode of dust in sinter fume, have impact on 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 low temperature ammonia process to carry out desulfurization, mend the position of ammonia in spraying layer, bias toward the top of whole desulfurizing tower, ammonia is easily caused also not have complete reaction, namely escape along with flue gas volatilization, therefore the loss phenomenon of ammonia is more serious; And total system employing is first carry out sulfite oxidation, then flow process ammonium sulfate being concentrated, filters.Containing dust in ammonium sulfite solution, can reduce oxidation efficiency, sulphur ammonium transforms not exclusively, affects the purity of product.Ammonium sulfate, in concentration process, absorbs the part sulfur dioxide in flue gas and solution acidic is strengthened, causing the aggravation to rear class equipment corrosion; Most of dust simultaneously in flue gas can enter in solution and form colloidal state with ammonium sulfate, and because ammonium sulfate concentration becomes large, makes filter operation more difficult; The filter residue filtered does not have processing scheme, not only can form new pollution, and affect the overall productivity of ammonium sulfate.

Summary of the invention

The present invention is directed to existing sintering flue gas ammonia method desulfurizing system above shortcomings, a kind of sintering flue gas ammonia method desulfurizing system and technique are provided.

The technical scheme that the present invention solves the problems of the technologies described above is as follows: a kind of sintering flue gas ammonia method desulfurizing system comprises for ammonia system, absorption system, filtration system and oxidative system, the described ammonia system that supplies is connected with absorption system, described absorption system is connected with filtration system, and described filtration system is connected with oxidative system; The described ammonia system that supplies comprises liquefied ammonia feeding mechanism, with the ammonia absorber that described liquefied ammonia feeding mechanism is connected, the concentrated ammonia liquor storage tank be connected with described ammonia absorber, with the aqua ammonia pump that described concentrated ammonia liquor storage tank is connected, with the pipe-line mixer that described aqua ammonia pump is connected, the ammoniacal liquor surge tank be connected with described pipe-line mixer, and the confession ammonia pump be connected with described ammoniacal liquor surge tank; Described absorption system comprises reaction tower, the connection flue be connected with described reaction tower, and the scrubbing tower be connected with described connection flue, and described reaction tower is connected with for ammonia pump; Described filtration system comprises the turbid liquid pump that to be connected with described scrubbing tower, the turbid liquid centrifuge be connected with described turbid liquid pump, the filtration pans be connected with described turbid liquid centrifuge and excessively filter residue flow container, with the clear liquid pump that described filtration pans are connected, with the accurate filter that described clear liquid pump is connected, with the described filter pressing pump crossed filter residue flow container and be connected, and the filter press be connected with described filter pressing pump, described filter residue flow container of crossing is connected with accurate filter; Described oxidative system comprises the oxidizing tower be connected with described accurate filter, and the oxidation fan be connected with described oxidizing tower.

The invention has the beneficial effects as follows: sintering flue gas ammonia method desulfurizing system of the present invention can not only remove the sulfur dioxide in flue gas effectively, and reduce the escape degree of ammonia, the accessory substance ammonium sulfite generated carries out low concentration atmospheric pressure oxidation after filtering and impurity removing, ensure the conversion ratio of ammonium sulfate, for the ammonium sulfate preparation system of rear class provides qualified material solution; Sintering flue gas ammonia method desulfurizing system of the present invention rational in infrastructure, make flue gas qualified discharge and reduce escape ammonia produce secondary pollution, by first filtering the accessory substance processing procedure in early stage of rear oxidation, for the ammonium sulfate preparation system of rear class provides qualified material liquid, ensure that 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 described reaction tower is connected with smoke inlet, and described reaction tower is positioned at the top connecting flue and comprises tubular reactor, and described tubular reactor comprises ammonia spray device, and described tubular reactor is connected with for ammonia pump; Described reaction tower is positioned at and connects the bottom of flue and comprise washing liquid bath, described washing liquid bath by dividing plate be connected flue and separate.

Further, the top of described scrubbing tower is connected with exhanst gas outlet, and described scrubbing tower is positioned at the top connecting flue and is divided into dehydrating demisting section from top to bottom, washes ammonia section and washing section; Described scrubbing tower is positioned at the bottom connecting flue and comprises slurries memory block.

Further, described dehydrating demisting section and wash ammonia section and formed by the first baffle for separating, described first dividing plate has multiple first gas cap towards one end of dehydrating demisting section; Describedly wash ammonia section and washing section is separated by second partition, described second partition has multiple second gas cap towards the one end washing ammonia section.

Further, described dehydrating demisting section comprises at least one demister; Described ammonia section of washing comprises at least one deck cleaning solution spray equipment; Described washing section comprises at least one deck slurries spray equipment, and is positioned at the air ducting below slurries spray equipment, described air ducting be connected flue correspondence arrange.

Further, described first dividing plate is connected with washing liquid bath respectively by pipeline with second partition.

Further, described washing liquid bath is connected with slurry tank with cleaning solution spray equipment respectively by detergent circulator, and described slurries memory block is connected with slurries spray equipment by slurry circulating pump.

Further, described oxidative system also comprises aeration cycle pump and sulphur ammonium liquid storage tank, the bottom of described oxidizing tower is connected with the top of oxidizing tower by aeration cycle pump, simultaneously, described sulphur ammonium liquid storage tank is connected with the bottom of oxidizing tower, the inwall of described oxidizing tower is provided with heat exchanger, and described heat exchanger circumferentially distributes along the radial direction of oxidizing tower.

The present invention also provides a kind of technical scheme solved the problems of the technologies described above as follows: a kind of sintering flue gas ammonia method desulfurizing technique comprises the following steps:

A. the liquefied ammonia in liquefied ammonia feeding mechanism is changed into concentration by ammonia absorber be the concentrated ammonia liquor of 15% ~ 25% and put into concentrated ammonia liquor storage tank and store;

B. the concentrated ammonia liquor in concentrated ammonia liquor storage tank is extracted out by aqua ammonia pump and be transported to mix with fresh water (FW) in pipe-line mixer after be delivered to ammoniacal liquor surge tank and carry out buffer memory;

C. the mixed liquor of concentrated ammonia liquor and fresh water (FW) is transported in reaction tower by supplying ammonia pump, itself and the sinter fume entered in reaction tower is made to carry out reacting and heat exchange, in reaction tower, temperature is between 55 DEG C ~ 150 DEG C, flue gas is no more than 2 seconds at reaction dwell time in the tower, and the inwall of tubular reactor has corrosion resistance;

D. reacted sinter fume enters in scrubbing tower by connecting flue, after entering the washing section in scrubbing tower successively, washing ammonia section and dehydrating demisting section, discharge from scrubber overhead, washing section is for the ammonium sulfite particle in the reacted sinter fume of spray-absorption and dust, slurry storage after spray is positioned at scrubbing tower and connects the lower slurry memory block of flue, and washing section and the liquid-gas ratio washing ammonia section control between 1 ~ 10;

E. the slurries containing ammonium sulfite are delivered to turbid liquid centrifuge by turbid liquid pump to carry out single filter and obtain filtrate and filter residue, and filtrate is delivered to filtration pans, filter residue was delivered to filter residue flow container;

F. filtrate is extracted out by clear liquid pump from filtration pans and is delivered to accurate filter and carry out cascade filtration and obtain clear liquid and filter residue, and clear liquid is delivered in oxidizing tower carries out aerating oxidation, backwashing water is delivered to accurate filter to make filter residue backwash out form slag liquid to be delivered to filter residue flow container, by filter pressing pump, slag liquid is delivered to filter press and carries out press filtration, in oxidizing tower, fluid temperature is no more than 60 DEG C, the air through dedusting is used to be oxidized in oxidizing tower, maintain coefficient of excess air between 1.25 ~ 2, ensure that liquid is not less than 6 hours at oxidation dwell time in the tower.

Further, the bottom of described oxidizing tower is connected with the top of oxidizing tower by aeration cycle pump, circulated sprinkling is carried out on the top being delivered to oxidizing tower after being extracted from oxidizing tower bottom by the clear liquid be delivered in oxidizing tower, simultaneously, the bottom of described oxidizing tower is connected with sulphur ammonium liquid storage tank, the clear liquid after oxidation is delivered to sulphur ammonium liquid storage tank and deposits.

Accompanying drawing explanation

Fig. 1 is the structural representation of sintering flue gas ammonia method desulfurizing system of the present invention.

Detailed description of the invention

Be described principle of the present invention and feature below in conjunction with accompanying drawing, example, only for explaining the present invention, is not intended to limit scope of the present invention.Fresh water (FW) in Fig. 1 refers to the deionized water through water softening device process.Flushing water refers to manufacture water.Backwash water refers to the industry water through multistage filtering, and impurities in water particle diameter is no more than 0.3 micron.Recirculated water refers to industrial in order to reasonable employment water resource, utilizes feature that water specific heat is larger as heating agent carrier, and cold water goes to absorb after heat heats up into hot water, then hot water is become cold water to recycle by cooling means.

As shown in Figure 1, the concentrated ammonia liquor that liquefied ammonia feeding mechanism and external liquefied ammonia tank vehicle are transformed into about about 20% by ammonia absorber 1 is placed on storage in concentrated ammonia liquor storage tank 3.When concentrated ammonia liquor is drawn through pipe-line mixer 6 by aqua ammonia pump and fresh water (FW) be mixed into the concentration of instructions for use after enter ammoniacal liquor surge tank 5 buffer memory, then by ammonia spray device 7 atomized spray delivered to for ammonia pump 4 in the tubular reactor 8 of reaction tower 10.Sinter fume enters from the smoke inlet 9 on reaction tower 10 top, in tubular reactor 8, and the SO in flue gas 2ammoniacal liquor after the atomization of spraying with ammonia spray device 7 reacts and heat exchange, completes desulphurization and denitration effect.The connection flue 21 of flue gas after desulfurization between double tower enters into scrubbing tower 11.Reaction tower lower space is washing liquid bath 22, with dividing plate be connected flue and separate.

Scrubbing tower 11 is multistage washing tower, and flue gas enters by connecting flue 21, upwards flows through washing section 18, washes ammonia section 16, after dehydrating demisting section 13, discharges from the exhanst gas outlet 12 on scrubbing tower 11 top through air ducting 20.The space connecting flue 21 entrance scrubbing tower bottom is slurries memory block, stores loop slurry and uses.Scrubbing tower 11 is separated into dehydrating demisting section 13 by gas cap 14 and dividing plate 15 from top to bottom, washes ammonia section 16, washing section 18 3 functional areas, is used for respectively removing the dirt in water smoke, escape ammonia, sulphur ammonium particle and flue gas.The effect of dividing plate 15 flushing water and cleaning solution is back to washing liquid bath 22, and gas cap 14 plays and ventilates and be uniformly distributed the effect of flue gas.Wash ammonium through washing section dedusting, wash ammonia section trapping escape ammonia after flue gas after dehydrating demisting section 13 is removed fine drop by demister, enter air.With flushing water, periodic cleaning is carried out to demister.Wash the cleaning solution spray equipment 17 having more than one deck in ammonia section 16.Cleaning solution spray equipment 17 forms with washing liquid bath 22 and cleaning circulation pump 23 functional areas that a washing removes escape ammonia.After cleaning solution concentration reaches finite concentration, portion washes liquid is transported to scrubbing tower bottom, as the replenisher of loop slurry through cleaning circulation pump 23 to the lateral of the main pipeline of spray equipment 17.Multilayer slurries spray equipment 19 is had in washing section 18, slurries in slurries memory block are extracted by slurry circulating pump 24, carry out atomizing spray through Cemented filling to slurries spray equipment 19, the slurries sprayed absorb desulfurization product ammonium sulfite particle and dust in washing flue gas.After ammonium sulfite concentration in slurries reaches technological requirement index, extracted out by turbid liquid pump and deliver to the separation that filtration system carries out dirt mud.Described dehydrating demisting section 13 according to process condition adjustment spray washing intensity and frequency, described in wash ammonia section 16 and washing section 18 spray flux reasonably regulate 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 single filter, and pans 35 filter in filtrate entering, and filter residue removed filter residue flow container 26.Single filter liquid is extracted out by clear liquid pump 34 from filtration pans 35, delivers to accurate filter 33 and carries out cascade filtration.Deliver to oxidizing tower 31 from accurate filter clear liquid out and carry out aerating oxidation, utilize backwash water backwash to wash the filter residue come from accurate filter and entered into filter residue flow container 26.The slag liquid crossed in filter residue flow container 26 is delivered to filter press 28 and is carried out press filtration by filter pressing pump 27, and filtrate returns filtration pans, and stock ground delivered to by filter cake.

After entering oxidizing tower 31 from accurate filter 33 clear liquid out, the air oxidation of oxidizing tower sent into by oxidized blower fan 29, in order to reach higher oxidation efficiency, to extract solution deliver to oxidizing tower top and carry out circulated sprinkling with aeration cycle pump 30 from oxidizing tower bottom.Oxidizing tower is built-in with recuperator, and the radial direction on the inwall that described heat exchanger is arranged on oxidizing tower and along oxidizing tower circumferentially distributes, and regulates circulating water flow to control under reasonable conditions to make oxidizing temperature.Well-oxygenated ammonium sulfate is delivered to sulphur ammonium liquid storage tank 32 by 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 desulfurizing agent according to ammoniacal liquor, then ammonia absorber 1 and aqua ammonia pump 2 can omit, and tubular reactor 8 can be single tube also can be multitube combination, and washing liquid bath 22 can separate to set up with reaction tower 10 becomes independent equipment.

Sintering flue gas ammonia method desulfurizing technique of the present invention adopts desulphurization reaction, washes the flow process of ammonium deamination, filtering and impurity removing, the clean ammonium of oxidation, make technique science, rationally more, adopt reaction tower to be separated outfit with scrubbing tower, contribute to actual use and adapt to the desulfurization demand of large scale sintering equipment.

Have employed multi-layer classification spray washing in scrubbing tower in sintering flue gas ammonia method desulfurizing system of the present invention, absorb the measure of escape ammonia, reduce the secondary pollution problem that escape ammonia causes; For sinter fume dust feature, the Multistage filtering device that concentration is adjustable is set, effectively removes metallic dust and recycle and reuse; Adopt efficient oxidation tower, improve the conversion ratio of ammonium salt, reduce superfluous air quantity, save energy consumption; Forced oxidation section, adopts the mode of gas-liquid counter current and the efficient tower tray of mass transfer to carry out further accelerating oxidation effect, makes the conversion ratio of ammonium sulfite remain on higher level; Adopt ammonia absorber rapidly liquefied ammonia to be changed into concentrated ammonia liquor to deposit, the potential safety hazard avoiding liquefied ammonia storage to bring and too much place take, and use if metallurgical integrated complex has self-produced ammoniacal liquor directly to receive with concentrated ammonia liquor storage tank, ammonia absorber 1 and aqua ammonia pump 2 can omit.

The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.

Claims (9)

1. a sintering flue gas ammonia method desulfurizing technique, is characterized in that, comprises the following steps:
A. the liquefied ammonia in liquefied ammonia feeding mechanism is changed into concentration by ammonia absorber be the concentrated ammonia liquor of 15% ~ 25% and put into concentrated ammonia liquor storage tank and store;
B. the concentrated ammonia liquor in concentrated ammonia liquor storage tank is extracted out by aqua ammonia pump and be transported to mix with fresh water (FW) in pipe-line mixer after be delivered to ammoniacal liquor surge tank and carry out buffer memory;
C. the mixed liquor of concentrated ammonia liquor and fresh water (FW) is transported in reaction tower by supplying ammonia pump, itself and the sinter fume entered in reaction tower is made to carry out reacting and heat exchange, in reaction tower, temperature is between 55 DEG C ~ 150 DEG C, flue gas is no more than 2 seconds at reaction dwell time in the tower, and the inwall of tubular reactor has corrosion resistance;
D. reacted sinter fume enters in scrubbing tower by connecting flue, after entering the washing section in scrubbing tower successively, washing ammonia section and dehydrating demisting section, discharge from scrubber overhead, washing section is for the ammonium sulfite particle in the reacted sinter fume of spray-absorption and dust, slurry storage after spray is positioned at scrubbing tower and connects the lower slurry memory block of flue, and washing section and the liquid-gas ratio washing ammonia section control between 1 ~ 10;
E. the slurries containing ammonium sulfite are delivered to turbid liquid centrifuge by turbid liquid pump to carry out single filter and obtain filtrate and filter residue, and filtrate is delivered to filtration pans, filter residue was delivered to filter residue flow container;
F. filtrate is extracted out by clear liquid pump from filtration pans and is delivered to accurate filter and carry out cascade filtration and obtain clear liquid and filter residue, and clear liquid is delivered in oxidizing tower carries out aerating oxidation, backwashing water is delivered to accurate filter to make filter residue backwash out form slag liquid to be delivered to filter residue flow container, by filter pressing pump, slag liquid is delivered to filter press and carries out press filtration, in oxidizing tower, fluid temperature is no more than 60 DEG C, the air through dedusting is used to be oxidized in oxidizing tower, maintain coefficient of excess air between 1.25 ~ 2, ensure that liquid is not less than 6 hours at oxidation dwell time in the tower.
2. sintering flue gas ammonia method desulfurizing technique according to claim 1, it is characterized in that, the bottom of described oxidizing tower is connected with the top of oxidizing tower by aeration cycle pump, circulated sprinkling is carried out on the top being delivered to oxidizing tower after being extracted from oxidizing tower bottom by the clear liquid be delivered in oxidizing tower, simultaneously, the bottom of described oxidizing tower is connected with sulphur ammonium liquid storage tank, the clear liquid after oxidation is delivered to sulphur ammonium liquid storage tank and deposits.
3. one kind for realizing the sintering flue gas ammonia method desulfurizing system of sintering flue gas ammonia method desulfurizing technique as claimed in claim 1 or 2, it is characterized in that, comprise for ammonia system, absorption system, filtration system and oxidative system, the described ammonia system that supplies is connected with absorption system, described absorption system is connected with filtration system, and described filtration system is connected with oxidative system; The described ammonia system that supplies comprises liquefied ammonia feeding mechanism, with the ammonia absorber that described liquefied ammonia feeding mechanism is connected, the concentrated ammonia liquor storage tank be connected with described ammonia absorber, with the aqua ammonia pump that described concentrated ammonia liquor storage tank is connected, with the pipe-line mixer that described aqua ammonia pump is connected, the ammoniacal liquor surge tank be connected with described pipe-line mixer, and the confession ammonia pump be connected with described ammoniacal liquor surge tank; Described absorption system comprises reaction tower, the connection flue be connected with described reaction tower, and the scrubbing tower to be connected with described connection flue, the top of described reaction tower is connected with smoke inlet, described reaction tower is positioned at the top connecting flue and comprises tubular reactor, described tubular reactor comprises ammonia spray device, and described tubular reactor is connected with for ammonia pump; Described reaction tower is positioned at and connects the bottom of flue and comprise washing liquid bath, described washing liquid bath by dividing plate be connected flue and separate; Described filtration system comprises the turbid liquid pump that to be connected with described scrubbing tower, the turbid liquid centrifuge be connected with described turbid liquid pump, the filtration pans be connected with described turbid liquid centrifuge and excessively filter residue flow container, with the clear liquid pump that described filtration pans are connected, with the accurate filter that described clear liquid pump is connected, with the described filter pressing pump crossed filter residue flow container and be connected, and the filter press be connected with described filter pressing pump, described filter residue flow container of crossing is connected with accurate filter; Described oxidative system comprises the oxidizing tower be connected with described accurate filter, and the oxidation fan be connected with described oxidizing tower.
4. sintering flue gas ammonia method desulfurizing system according to claim 3, is characterized in that, the top of described scrubbing tower is connected with exhanst gas outlet, and described scrubbing tower is positioned at the top connecting flue and is divided into dehydrating demisting section from top to bottom, washes ammonia section and washing section; Described scrubbing tower is positioned at the bottom connecting flue and comprises slurries memory block.
5. sintering flue gas ammonia method desulfurizing system according to claim 4, is characterized in that, described dehydrating demisting section and wash ammonia section and formed by the first baffle for separating, and described first dividing plate has multiple first gas cap towards one end of dehydrating demisting section; Describedly wash ammonia section and washing section is separated by second partition, described second partition has multiple second gas cap towards the one end washing ammonia section.
6. the sintering flue gas ammonia method desulfurizing system according to claim 4 or 5, is characterized in that, described dehydrating demisting section comprises at least one demister; Described ammonia section of washing comprises at least one deck cleaning solution spray equipment; Described washing section comprises at least one deck slurries spray equipment, and is positioned at the air ducting below slurries spray equipment, described air ducting be connected flue correspondence arrange.
7. sintering flue gas ammonia method desulfurizing system according to claim 5, is characterized in that, described first dividing plate is connected with washing liquid bath respectively by pipeline with second partition.
8. sintering flue gas ammonia method desulfurizing system according to claim 6, it is characterized in that, described washing liquid bath is connected with slurries memory block with cleaning solution spray equipment respectively by detergent circulator, and described slurries memory block is connected with slurries spray equipment by slurry circulating pump.
9. sintering flue gas ammonia method desulfurizing system according to claim 3, it is characterized in that, described oxidative system also comprises aeration cycle pump and sulphur ammonium liquid storage tank, the bottom of described oxidizing tower is connected with the top of oxidizing tower by aeration cycle pump, simultaneously, described sulphur ammonium liquid storage tank is connected with the bottom of oxidizing tower, and the inwall of described oxidizing tower is provided with heat exchanger, and described heat exchanger circumferentially distributes along the radial direction of oxidizing tower.
CN201010614694.XA 2010-12-30 2010-12-30 Sintering flue gas ammonia desulfurization system and process CN102527210B (en)

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Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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
CN103820171B (en) * 2014-03-12 2016-03-16 邯郸市裕泰燃气有限公司 Gas desulfurizer
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

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN201208544Y (en) * 2008-06-13 2009-03-18 江苏和亿昌环保有限公司 Desulfuration absorbing tower with dual-tower structure
CN101433798A (en) * 2007-11-12 2009-05-20 河南省旭辉环保工程有限公司 High-efficient wet-type ammonia recovering method desulfuration method with oxidation and concentration processes outside tower and device thereof
CN201357043Y (en) * 2008-12-31 2009-12-09 宁波金远东工业科技有限公司 Device for removing sulfur dioxide from waste gas
CN201543375U (en) * 2009-12-04 2010-08-11 王建敏 Amino flue gas desulfuration device
CN101862583A (en) * 2009-09-27 2010-10-20 北京九州美电环保工程有限公司 Flue gas desulfurization process suitable for sintering machine of steel mill
CN101898081A (en) * 2010-08-04 2010-12-01 山西新唐工程设计有限公司 Method for desulphurizing sulfur-containing flue gas with coking crude gas water-washing deaminized ammonia water
CN201669043U (en) * 2009-11-19 2010-12-15 娄爱娟 Ammonia flue gas desulfurization device

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101433798A (en) * 2007-11-12 2009-05-20 河南省旭辉环保工程有限公司 High-efficient wet-type ammonia recovering method desulfuration method with oxidation and concentration processes outside tower and device thereof
CN201208544Y (en) * 2008-06-13 2009-03-18 江苏和亿昌环保有限公司 Desulfuration absorbing tower with dual-tower structure
CN201357043Y (en) * 2008-12-31 2009-12-09 宁波金远东工业科技有限公司 Device for removing sulfur dioxide from waste gas
CN101862583A (en) * 2009-09-27 2010-10-20 北京九州美电环保工程有限公司 Flue gas desulfurization process suitable for sintering machine of steel mill
CN201669043U (en) * 2009-11-19 2010-12-15 娄爱娟 Ammonia flue gas desulfurization device
CN201543375U (en) * 2009-12-04 2010-08-11 王建敏 Amino flue gas desulfuration device
CN101898081A (en) * 2010-08-04 2010-12-01 山西新唐工程设计有限公司 Method for desulphurizing sulfur-containing flue gas with coking crude gas water-washing deaminized ammonia water

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