CN200998639Y - Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower - Google Patents

Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower Download PDF

Info

Publication number
CN200998639Y
CN200998639Y CNU2007200671849U CN200720067184U CN200998639Y CN 200998639 Y CN200998639 Y CN 200998639Y CN U2007200671849 U CNU2007200671849 U CN U2007200671849U CN 200720067184 U CN200720067184 U CN 200720067184U CN 200998639 Y CN200998639 Y CN 200998639Y
Authority
CN
China
Prior art keywords
tower
condensing crystallizing
absorption
desulfurizing tower
circulation fluid
Prior art date
Application number
CNU2007200671849U
Other languages
Chinese (zh)
Inventor
李培生
Original Assignee
李培生
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 李培生 filed Critical 李培生
Priority to CNU2007200671849U priority Critical patent/CN200998639Y/en
Application granted granted Critical
Publication of CN200998639Y publication Critical patent/CN200998639Y/en

Links

Abstract

The utility model provides a combined type ammonia desulfurization tower for condensation crystallization and absorption oxidization combination, which provides a novel ammonia desulfurization device with low energy consumption and reliable running. The utility model comprises a desulfurization tower, a condensation and crystallization tower and a connecting pipe for connecting the desulfurization tower with a condensation and crystallization tower, wherein the desulfurization is performed to entering fume in the desulfurization tower, generated ammonium sulfate solution is taken as absorption circulating liquid in the device, clean fume is exhausted, the desulfurization tower comprises a demisting section, an absorption section, a cooling section, and an oxidization section; before entering into the desulfurization tower, the fume to be desulfurized firstly enters into the condensation and crystallization tower, the ammonium sulfate solution generated in the desulfurization tower is condensed, saturated, and crystallized, and becomes the slurry to be discharged, the condensation and crystallization tower comprises a fume inlet opening, a distributor with the nozzle, and a crystallizing tank for condensing, saturating, and crystallizing the ammonium sulfate solution. The utility model has high device desulfurization rate, high utilization rate of absorption agent, and no secondary pollution, simultaneously the generated ammonium sulfate solution is evaporated and condensed by utilizing the heat of hot fume to be saturated and crystallized, and the energy consumption required for the subsequent processing of the ammonium sulfate solution is greatly reduced.

Description

Condensing crystallizing and absorption oxide compound formula ammonia process of desulfurization tower

Technical field

The utility model relates to a kind of condensing crystallizing and absorbs oxide compound formula ammonia process of desulfurization tower.

Background technology

China coal-burning power plant is numerous, and the medium and small unit that enterprises such as particularly heat supply, large-scale petrochemical, chemical industry, metallurgy have (the 100MW unit is following) spreads all over the place especially.The coal-fired SO that produces 2Cause severe contamination to atmosphere, for reducing SO 2Harm, the newly-built coal-fired plant boiler of national requirements must be built flue gas desulfur device simultaneously, and power plant also wants undertaking treatment within a prescribed limit of time in labour.Because the desulfurizer investment is bigger, leading at present desulfurization method of limestone-gypsum technology, medium and small steam power plant is difficult to bear, and operating cost is higher, and the desulfurizing byproduct gypsum is subjected to the restriction of quality, output and cost, and purposes is limited, causes extra processing cost.Therefore seek a kind ofly to compare with the calcium method, have lower operating cost, the ammonia desulfurizing process of producing ammonium sulfate byproduct chemical fertilizer will reduce the flue gas desulfurization cost greatly simultaneously.

At present, more domestic arcolas adopt a kind of easy ammonia process spray column desulfurizer, adopt directly to spray with ammoniacal liquor on the top of tower, but because spray flux is few, flue-gas temperature height (~100 ℃), the ammoniacal liquor highly volatile makes discharged flue gas carry a large amount of free ammonias secretly in addition, and desulfuration efficiency is extremely low, be difficult to reclaim sulfuric acid ammonium product, cause desulfurizing agent to run off in a large number, the operating cost height, but also formed the secondary pollution of ammonia.

More external companies, adopt the ammonia desulfuration equipment of spray column technology, owing to will satisfy higher mass transfer, heat transfer requirement, so the liquid-gas ratio of desulfurizing tower is very big, near desulfurization method of limestone-gypsum technology, make that the flow that absorbs circulation fluid is very big, energy consumption is bigger, carry secretly seriously owing to liquid film simultaneously, the demist of desulfurizing tower requires very high, even has adopted electric demist, whole in addition device requirement for anticorrosion height, the construction costs that makes the ammonia process of desulfurization than equal desulfurization method of limestone-gypsum technology taller~20%, seriously restricted the popularization of ammonia-process desulfurization technique.

The utility model content

The purpose of this utility model is a kind of condensing crystallizing of design and absorbs oxide compound formula ammonia process of desulfurization tower, to overcome the shortcoming and defect that existing ammonia type flue gas desulfurizing apparatus exists, provides a kind of energy consumption low, reliable novel ammonia desulfuration equipment.

In order to realize the purpose of this utility model, condensing crystallizing of the present utility model and absorption oxide compound formula ammonia process of desulfurization tower comprise:

A kind of condensing crystallizing and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that comprising:

Desulfurizing tower, condensing crystallizing tower and connect described desulfurizing tower and the tube connector of condensing crystallizing tower;

Described desulfurizing tower comprises:

The top of described desulfurizing tower is absorber portion;

The demist section is set on described absorber portion, and is with automatic cleaning spraying device, to produce clean flue gas, the water of described spray equipment is provided by a water pump;

The top of described desulfurizing tower is provided with exhanst gas outlet, to discharge described clean flue gas;

The bottom of described desulfurizing tower is provided with oxidation panel, oxidation panel adopts oxidation pond, described oxidation panel bottom is provided with the compressed-air actuated compressed air inlet of input, make the ammonium sulfite solution that absorbs the flue gas generation be oxidized to ammonium sulfate, this ammonium sulfate is for absorbing circulation fluid, and described oxidation panel top is provided with and absorbs the circulation fluid outlet;

Described absorption circulation fluid outlet is connected with a circulating tank by pipe, described circulating tank has the ammoniacal liquor input, the bottom of described circulating tank is provided with the absorption liquid circulating pump, and the absorption liquid circulating pump absorbs the circulation fluid inlet by pipe and first of the absorber portion that is arranged at described desulfurizing tower and is connected;

The absorption circulation fluid inlet of described absorber portion is connected with groove type distributor;

Described absorber portion bottom is provided with collecting tank, be used to collect and absorb circulation fluid and will absorb the oxidation panel that circulation fluid is sent into desulfurizing tower, and the oxidation panel overflow that the absorption circulation fluid that makes gravity flow can pass through desulfurizing tower is finished the absorption oxidation cycle process of absorption liquid to circulating tank;

Described condensing crystallizing tower comprises:

The below of described condensing crystallizing tower is equipped with the smoke inlet that flue gas to be desulfurization enters;

The top of described condensing crystallizing tower is equipped with distributor, and described distributor is provided with nozzle, sprays into the ammonium sulfate that generates from described desulfurizing tower, makes the flue gas humidifying cooling that enters, and the flue gas of cooling enters described desulfurizing tower by described tube connector;

The distributor below of described condensing crystallizing tower is provided with second and absorbs the circulation fluid inlet, and described second absorbs the circulation fluid inlet is connected by the tank connected absorption liquid circulating pump of pipe and described circulation;

The bottom of described condensing crystallizing tower is provided with the crystallizing pond that makes ammonium sulfate concentrate saturated crystallization, the bottom of described crystallizing pond is provided with the condensing crystallizing circulating pump, the bottom of described crystallizing pond also is provided with the slurries outlet, the middle part of described condensing crystallizing tower is provided with the 3rd and absorbs the circulation fluid inlet, described condensing crystallizing circulating pump absorbs the circulation fluid inlet by pipe and the described the 3rd and is connected, make the interior mother liquor of described crystallizing pond return described condensing crystallizing tower, and the slurries of crystallization are discharged by described slurries outlet.

The absorber portion of described desulfurizing tower adopts three sections to mix structured packing, and described mixing structured packing is 160~250 model, and material is a polypropylene.

The demist section of described desulfurizing tower adopts the corrugated plating demister, and material is a polypropylene.

First of described desulfurizing tower absorbs the circulation fluid inlet two.

The material of the groove type distributor of described desulfurizing tower adopts polypropylene or fiberglass.

The collecting tank of described desulfurizing tower absorber portion bottom is an oxidation panel of described absorption circulation fluid being sent into described desulfurizing tower by an outer connecting leg.

The distributor pipe of punching is set in place, described compressed air inlet in the oxidation panel of described desulfurizing tower.

The distributor of described condensing crystallizing tower adopts the injecting type distributor, single setting, and the nozzle on the described distributor adopts 19 or 37 or 61 solid cone spray nozzles.

Also be equipped with an agitator in the crystallizing pond of described condensing crystallizing tower.

Effect of the present utility model:

Condensing crystallizing of the present utility model and absorption oxide compound formula ammonia process of desulfurization tower are low, the reliable novel ammonia desulfuration equipments of a kind of energy consumption.Adopt condensing crystallizing in addition, absorb oxide compound formula ammonia process of desulfurization tower, the purifying rate of major pollutants can reach in the flue gas: SO 2: 90~99.5%; SO 3: 30~50%; HCl:90~100%; HF:95~100%; NOX:10~30%; Dirt: 45~75%.

For further specifying above-mentioned purpose of the present utility model, design feature and effect, the utility model is described in detail below with reference to accompanying drawing.

Description of drawings

Fig. 1 is condensing crystallizing of the present utility model and the structural representation that absorbs oxide compound formula desulfurizing tower.

The symbol description of critical piece in the accompanying drawing:

1, desulfurizing tower 2, collecting tank

3, absorber portion 4, demist section

5, oxidation panel 6, circulating tank

7, condensing crystallizing tower 8, distributor

9, agitator 10, crystallizing pond

11, spray equipment 12, absorption liquid circulating pump

13, condensing crystallizing circulating pump 14, tube connector

15, smoke inlet 16, dividing plate

17, exhanst gas outlet 18, compressed air inlet

19, absorb circulation fluid outlet 20, the first and absorb the circulation fluid inlet

21, the second absorb circulation fluid inlet 22, the three absorbs the circulation fluid inlet

23, slurries outlet 24, outer connecting leg

Specific implementation method

Be elaborated below in conjunction with the specific embodiment of accompanying drawing to condensing crystallizing of the present utility model and absorption oxide compound formula ammonia process of desulfurization tower.

Referring to Fig. 1, Fig. 1 is condensing crystallizing of the present utility model and the structural representation that absorbs oxide compound formula ammonia process of desulfurization tower.As shown in Figure 1, the utility model mainly comprises:

Desulfurizing tower 1, condensing crystallizing tower 7 etc.

Described desulfurizing tower 1 is by the countercurrent filling tower design, adopt heat transfer, the good block-resisting type structured packing of mass transfer effect, therefore, compare the spray column that traditional wet desulphurization is adopted, liquid-gas ratio falls and can reduce by 8~10 times, reduces the power of required absorption liquid circulating pump greatly.

Comprise in the described desulfurizing tower 1:

The top of desulfurizing tower 1 is absorber portion 3, adopts three sections to mix structured packing, adopts 160~250 model respectively, and packed height is according to flue gas load and contained SO 2Amount is calculated and is determined.

Demist section 4 is set on absorber portion 3, and demist section 4 adopts the efficient demister of corrugated plating, and is with automatic cleaning spraying device 11, is provided with exhanst gas outlet 17 at the top of desulfurizing tower 1, and the clean flue gas of generation is discharged from exhanst gas outlet 17.Fresh water (FW) leads to the spray equipment 11 that desulfurizing tower 1 delivered to water by pump (not shown), the flushing water and the fume washing water of demist section 4 are provided, before desulfurizing tower 1 does not enter flue gas, this spray equipment 11 is with the oxidation panel 5 of desulfurizing tower 1 bottom and be located in the desulfurizing tower 1 outer loop jar 6 and fill with water, after waiting to need the flue gas of desulfurization to enter desulfurizing tower 1, become the absorption circulation fluid.

The bottom of desulfurizing tower 1 is provided with oxidation panel 5, separate with the absorber portion 3 of dividing plate 16 itself and tower, oxidation panel 5 adopts oxidation pond, be provided with the compressed-air actuated compressed air inlet 18 of input in the bottom of oxidation panel 5, in oxidation pond, import compressed air, make the ammonium sulfite solution that absorbs the flue gas generation be oxidized to ammonium sulfate (promptly, the above-mentioned absorption circulation fluid of mentioning), be provided with absorption circulation fluid outlet 19 on the top of oxidation panel 5, for improving the oxygenation efficiency of ammonium sulfite, 18 places are provided with the distributor pipe (not shown) of punching in the compressed air inlet in the oxidation panel 5 of desulfurizing tower 1, evenly carry oxidation air, and the pressure of oxidation air mentioned 0.15~0.25MPa, and guaranteeing to absorb mixed solution in the presence of high-concentration sulfuric acid ammonium (~35%), wherein contained sulfite oxidation rate still can reach 98%.The hole count of the height of oxidation air amount, oxidation pond, oxidation air distributor pipe and big young pathbreaker calculate according to factors such as the flow of flue gas, sulfur content, temperature and determine.。

Described absorption circulation fluid outlet 19 is connected with above-mentioned circulating tank 6 by pipe, make the absorption circulation fluid in the oxidation panel 5 enter circulating tank 6, circulating tank 6 adds ammoniacal liquor, the bottom of described circulating tank 6 is provided with absorption liquid circulating pump 12, absorption liquid circulating pump 12 absorbs circulation fluid inlet 20 by pipe and first of the absorber portion 3 that is arranged at described desulfurizing tower 1 and is connected, make ammoniacal liquor mix the back enters desulfurizing tower 1 by absorption liquid circulating pump 12 absorber portion 3 at circulating tank 6 with described absorption circulation fluid, present embodiment adopts two first absorption circulation fluids to enter the mouth at 20 o'clock, circulation fluid is sent into the absorber portion 3 of desulfurizing tower 1, divides two strands and enters in the tower.Ammoniacal liquor through aqua ammonia pump (not shown), and (is controlled at pH value: 5.0~5.9) regulate the ammoniacal liquor flow by the pH value that analyze to absorb circulation fluid by ammonia water tank (not shown).Absorb the collecting tank 2 that circulation fluid is provided with through absorber portion 3 bottoms of desulfurizing tower 1, collect and flow into certainly the oxidation panel 5 of desulfurizing tower 1 by the outer connecting leg 24 of tower, described absorber portion bottom is provided with collecting tank 2, be used to collect and absorb circulation fluid and it is sent into the oxidation panel of desulfurizing tower by the outer connecting leg 24 of tower, because collecting tank has enough height, make oxidation panel 5 overflows that the absorption circulation fluid of gravity flow can be by desulfurizing tower 1 to circulating tank 6, finish the absorption oxidation cycle process of absorption liquid.Blast compressed air with oxidation air compressor machine (not shown) by compressed air inlet 18 in the oxidation panel 5 and carry out oxidation, make the ammonium sulfite solution of generation be oxidized to ammonium sulfate.Air is by the absorber portion 3 that enters desulfurizing tower 1 communicating pipe (not shown) of desulfurizing tower 1.The ammonium sulfate overflow that forms at oxidation panel 5 is to absorption liquid circulating tank 6, and with absorption liquid circulating pump 12 circulation fluid sent into the absorber portion 3 of desulfurizing tower 1 in the bottom of absorption liquid circulating tank 6, divides two strands and enters in the tower.The ammonium sulfate that the absorption liquid of circulation utilizes the heat of vaporization moisture of hot flue gas and constantly generates, make ammonium sulfate concentration reach~20%, wherein, also contain a small amount of ammonium chloride etc.At absorption liquid circulating tank 6 usefulness absorption liquid circulating pumps 12 slurries delivery pumps ammonium sulfate is sent into condensing crystallizing tower 7 then.

Carry secretly for reducing liquid film, first of described absorber portion 3 absorbs circulation fluid inlet 20 and is connected with groove type distributor (not shown), be to enter desulfurizing tower 1 after groove type distributor enters absorber portion 3 by absorption liquid circulating pump 12 after described absorption circulation fluid mixes, the material of described groove type distributor adopts PP (polypropylene) or FRP (fiberglass).

For making full use of the heat of flue gas, condensing crystallizing tower 7 before entering desulfurizing tower 1, flue gas is set, condensing crystallizing tower 7 is communicated with above-mentioned desulfurizing tower 1 by tube connector 14, make hot flue gas earlier through condensing crystallizing tower 7, spray into the ammonium sulfate that generates from desulfurizing tower 1, make the flue gas humidifying cooling that enters, the structure and the function thereof of this condensing crystallizing tower 7 are as follows:

The below of condensing crystallizing tower 7 is equipped with the smoke inlet 15 that flue gas to be desulfurization enters.The desulfurization flue gas is regulated, is sent into condensing crystallizing tower 7 by smoke inlet 15 after booster fan (not shown) supercharging through baffle door (not shown).

The top of condensing crystallizing tower 7 is equipped with distributor 8, that is, condensing crystallizing tower 7 is designed to spray column, adopts injecting type distributor 8, and single setting according to the size of smoke treatment amount, is adopted 19,37,61 solid cone spray nozzles respectively, and the hydrojet Duplication is 30~40%.Distributor 8 is provided with nozzle, sprays into the ammonium sulfate (promptly absorb circulation fluid, when flue gas did not enter condensing crystallizing tower 7, this absorption circulation fluid was the water in the above-mentioned desulfurizing tower 1) that generates from desulfurizing tower 1, makes the flue gas humidifying cooling that enters.

Distributor 8 belows of described condensing crystallizing tower 7 are equipped with second and absorb circulation fluid inlet 21, described second absorbs circulation fluid inlet 21 is connected with the absorption liquid circulating pump 12 that described circulating tank 6 is connected by pipe (not shown), and the absorption circulation fluid that circulating tank 6 is exported enters in the condensing crystallizing tower 7.

The bottom of condensing crystallizing tower 7 is provided with the crystallizing pond 10 that makes ammonium sulfate concentrate saturated crystallization.The absorption circulation fluid that the nozzle of above-mentioned distributor 8 is discharged makes ammonium sulfate concentrate saturated crystallization in the humidifying cooling flue gas in crystallizing pond 10, the bottom of described crystallizing pond 10 is provided with condensing crystallizing circulating pump 13, the bottom of described crystallizing pond 10 also is provided with slurries outlet 23, the middle part of described condensing crystallizing tower 7 is provided with the 3rd and absorbs circulation fluid inlet 22, condensing crystallizing circulating pump 13 absorbs circulation fluid inlet 22 by pipe and the described the 3rd and is connected, make crystallizing pond 10 interior mother liquors return condensing crystallizing tower 7, about 2% o'clock of the magma solid content of liquid to be recycled, by above-mentioned slurries outlet 23 usefulness slurries excavationg pumps (not shown) slurries being sent into one-level cyclone (not shown) carries dense, make ammonium sulfate magma solid content reach 5~10%, sending into second cyclone (not shown) more further carries dense, make ammonium sulfate magma solid content up to~30%, send into centrifuge (not shown) then and separate, the ammonia sulfate crystal of discharging (moisture content~3%) drying, packing is outer sells.In crystallizing pond 10, also be equipped with an agitator 9 that stirs described slurry.

The flue-gas temperature of condensing crystallizing tower 7 is reduced to 75~90 ℃ by 120~160 ℃, enter desulfurizing tower 1 by above-mentioned tube connector 8, absorber portion 3 via filler is formed is entered demist section 4 after the ammonium salt solution of ammoniacal liquor and formation and the water absorption respectively, becomes cleaning of off-gas, leave desulfurizing tower 1,45~52 ℃ of exhaust temperatures enter flue gas heater (not shown) then, with the Steam Heating of 0.4~1.0MPa, flue-gas temperature is elevated to more than 70 ℃, enters smoke stack emission.

Condensing crystallizing of the present utility model, absorption oxide compound formula ammonia process of desulfurization tower have been realized six functions that sweetening process is required: utilize desulfurizing tower 1 to absorb flue gas SO 2, to the clean flue gas washing of flue gas ash removal, sulfite oxidation, desulfurization with dewater (mist) and utilize 7 pairs of ammonium sulfates of condensing crystallizing tower to concentrate saturated crystallization, its technical indicator is as follows:

SO 2Absorb (or deviating from) efficient: 90~99.5%,

Dust removing effects: 45~75%,

The foam (mist) that contains that purifies flue gas is measured :≤100mg/Nm3,

Purify ammonia content :≤10mg/Nm3 in the flue gas.

Desulfurization chemical reaction principle of the present utility model is as follows:

Nucleus equipment desulfurizing tower 1, condensing crystallizing tower 7 are hot flue gas and the intermediate equipment that produces ammonium sulfate.SO in the flue gas 2Be removed in desulfurizing tower 1, the pH value in the desulfurizing tower 1 is controlled at ammonium sulfate/sulfite solution of about 35% of 5.0~5.9, with SO 2Reaction, generate ammonium bisulfite/disulfate according to following reaction:

(1)SO 2+H 2OH 2SO 3

(2)H 2SO 3+(NH 4) 2SO 4NH 4HSO 4+NH 4HSO 3

(3)H 2SO 3+(NH 4) 2SO 32NH 4HSO 3

In reaction (1), SO in the flue gas 2Soluble in water, generate sulfurous acid.In reaction (2) and (3), the ammonium sulfate that dissolves in sulfurous acid and this solution/sulphite reaction.Join the ammoniacal liquor in the circulating absorption solution, as follows in and acid:

(4)H 2SO 3+NH 3NH 4HSO 4

(5)NH 4HSO 4+NH 3(NH 4) 2SO 3

(6)NH 4HSO 4+NH 3(NH 4) 2SO 4

Being ejected into the compressed air of desulfurizing tower 1 bottom oxidation panel 5, can be sulfate with sulfite oxidation in the following manner:

(NH 4) 2SO 3+1/2O 2→(NH 4) 2SO 4

At condensing crystallizing tower 7, after ammonium sulfate is saturated, ammonium sulfate is precipitated out from solution with crystal form.Heat of vaporization is provided in the following manner by the amount of residual heat will of flue gas:

(NH 4) 2SO 4(liquid state)+heat of vaporization → (NH 4) 2SO 4(solid)

Ammonium salt in condensing crystallizing tower 7 or be dissolved in the solution with ionic species, or be precipitated out with crystal form.Saved the evaporative crystallization operation of follow-up ammonium sulfate.

Desulfurizing tower 1, condensing crystallizing tower 7 adopts carbon steels to make, and the part of contact feed liquid adopts resinize phosphorus sheet or line with rubber anticorrosion, has reduced construction costs.Tower internals can adopt fiberglass (FRP) or polypropylene (PP) to make.

Limit because of the place as existing power plant, can't arrange two combined column, this device can be cancelled condensing crystallizing tower 7, desulfurizing tower 1 only is set, this moment can with the ammonium sulfate solution concentration that generates in the tower by~20% bring up to~35%, this solution is handled by follow-up evaporative crystallization device again and obtained ammonium sulfate products, obviously this process energy consumption (steam) will increase greatly.

Those of ordinary skill in the art will be appreciated that, above embodiment is used for illustrating the utility model, and be not to be used as qualification of the present utility model, as long as in connotation scope of the present utility model, all will drop in the scope of the utility model claims variation, the modification of the above embodiment.

Claims (9)

1, a kind of condensing crystallizing and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that comprising:
Desulfurizing tower, condensing crystallizing tower and connect described desulfurizing tower and the tube connector of condensing crystallizing tower;
Wherein, described desulfurizing tower comprises:
The top of described desulfurizing tower is absorber portion;
The demist section is set on described absorber portion, and is with automatic cleaning spraying device, to produce clean flue gas, the water of described spray equipment is provided by a water pump;
The top of described desulfurizing tower is provided with exhanst gas outlet, to discharge described clean flue gas;
The bottom of described desulfurizing tower is provided with oxidation panel, oxidation panel adopts oxidation pond, described oxidation panel bottom is provided with the compressed-air actuated compressed air inlet of input, make the ammonium sulfite solution that absorbs the flue gas generation be oxidized to ammonium sulfate, this ammonium sulfate is for absorbing circulation fluid, and described oxidation panel top is provided with and absorbs the circulation fluid outlet;
Described absorption circulation fluid outlet is connected with a circulating tank by pipe, described circulating tank has the ammoniacal liquor input, the bottom of described circulating tank is provided with the absorption liquid circulating pump, and the absorption liquid circulating pump absorbs the circulation fluid inlet by pipe and first of the absorber portion that is arranged at described desulfurizing tower and is connected;
The absorption circulation fluid inlet of described absorber portion is connected with groove type distributor;
Described absorber portion bottom is provided with collecting tank, is used to collect absorb circulation fluid and will absorb the oxidation panel that circulation fluid is sent into desulfurizing tower, and makes the absorption circulation fluid of gravity flow finish the absorption oxidation cycle process of absorption liquid by the oxidation panel overflow to circulating tank;
Wherein, described condensing crystallizing tower comprises:
The below of described condensing crystallizing tower is equipped with the smoke inlet that flue gas to be desulfurization enters;
The top of described condensing crystallizing tower is equipped with distributor, and described distributor is provided with nozzle, sprays into the ammonium sulfate that generates from described desulfurizing tower, makes the flue gas humidifying cooling that enters, and the flue gas of cooling enters described desulfurizing tower by described tube connector;
The distributor below of described condensing crystallizing tower is equipped with second and absorbs the circulation fluid inlet, and described second absorbs the circulation fluid inlet is connected by the tank connected absorption liquid circulating pump of pipe and described circulation;
The bottom of described condensing crystallizing tower is provided with the crystallizing pond that makes ammonium sulfate concentrate saturated crystallization, the bottom of described crystallizing pond is provided with the condensing crystallizing circulating pump, the bottom of described crystallizing pond also is provided with the slurries outlet, the middle part of described condensing crystallizing tower is provided with the 3rd and absorbs the circulation fluid inlet, described condensing crystallizing circulating pump absorbs the circulation fluid inlet by pipe and the described the 3rd and is connected, make the interior mother liquor of described crystallizing pond return described condensing crystallizing tower, and the slurries of crystallization are discharged by described slurries outlet.
2, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
The absorber portion of described desulfurizing tower adopts three sections to mix structured packing, and described mixing structured packing is 160~250 model, and material is a polypropylene.
3, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula desulfurizing tower is characterized in that:
The demist section of described desulfurizing tower adopts the corrugated plating demister, and material is a polypropylene.
4, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
First of described desulfurizing tower absorbs the circulation fluid inlet two.
5, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
The material of the groove type distributor of described desulfurizing tower adopts polypropylene or fiberglass.
6, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
The collecting tank of described desulfurizing tower absorber portion bottom is sent into described absorption circulation fluid by an outer connecting leg oxidation panel of described desulfurizing tower.
7, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
The distributor pipe of punching is set in place, described compressed air inlet in the oxidation panel of described desulfurizing tower.
8, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
The distributor of described condensing crystallizing tower adopts the injecting type distributor, single setting, and the nozzle on the described distributor adopts 19 or 37 or 61 solid cone spray nozzles.
9, condensing crystallizing as claimed in claim 1 and absorption oxide compound formula ammonia process of desulfurization tower is characterized in that:
Also be equipped with an agitator in the crystallizing pond of described condensing crystallizing tower.
CNU2007200671849U 2007-02-09 2007-02-09 Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower CN200998639Y (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CNU2007200671849U CN200998639Y (en) 2007-02-09 2007-02-09 Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CNU2007200671849U CN200998639Y (en) 2007-02-09 2007-02-09 Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower

Publications (1)

Publication Number Publication Date
CN200998639Y true CN200998639Y (en) 2008-01-02

Family

ID=39013047

Family Applications (1)

Application Number Title Priority Date Filing Date
CNU2007200671849U CN200998639Y (en) 2007-02-09 2007-02-09 Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower

Country Status (1)

Country Link
CN (1) CN200998639Y (en)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101780368A (en) * 2010-03-26 2010-07-21 张蕊 Low energy consumption flue gas wet desulphurization process
CN101844034A (en) * 2010-06-18 2010-09-29 宁波金远东工业科技有限公司 Device for removing sulfur dioxide from waste gas and producing ammonium sulfate byproduct
CN101306321B (en) * 2008-07-15 2011-02-16 李宝林 Coal smoke desulfurization and dust removal device and its use method
CN101670231B (en) * 2009-07-23 2011-08-24 何金整 Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization
CN101601964B (en) * 2009-06-03 2012-01-11 李鹏举 Ammonia flue gas desulfurization device
CN102559959A (en) * 2012-03-13 2012-07-11 武汉宜生机电技术工程有限公司 Blast furnace water granulated slag steam desulfuration and water recycling device
CN101837235B (en) * 2009-03-19 2012-08-29 北京九州美电科技有限公司 Low-consumption high-efficiency boiler flue gas desulfurization process
CN102847422A (en) * 2011-07-22 2013-01-02 上海克硫环保科技股份有限公司 Apparatus for desulfurizing smoke through ammonia process
CN102850092A (en) * 2011-08-31 2013-01-02 上海克硫环保科技股份有限公司 Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof
CN103263841A (en) * 2013-05-27 2013-08-28 史永军 Method for removing aerosol in ammonia washing desulphurization of flue gas
CN101757844B (en) * 2008-12-24 2013-12-04 中石化宁波工程有限公司 Method and device for performing flue gas desulfurization by using ammonia process
CN104368223A (en) * 2014-11-07 2015-02-25 广德瑞邦涂料有限公司 Waste gas absorption device for synthesizing anodic electrophoretic paint resin
CN104482778A (en) * 2014-12-12 2015-04-01 湖南科技大学 Device and method for treating and using fume waste heat during harmful tail gas treatment
CN105311937A (en) * 2014-06-11 2016-02-10 成都新筑展博环保科技有限公司 Method of producing ammonium sulfate through flue gas desulfurization
CN105854562A (en) * 2016-05-14 2016-08-17 张波 Ultralow-emission desulfurization absorption device
CN106823740A (en) * 2017-01-23 2017-06-13 上海大学 Charcoal element stove, the ammonia process of desulfurization of coke oven flue gas multisection type and dedusting absorption tower
CN107261789A (en) * 2017-06-15 2017-10-20 上海交通大学 The ammonia method desulfurizing system and method for a kind of high-sulfur flue gas

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101306321B (en) * 2008-07-15 2011-02-16 李宝林 Coal smoke desulfurization and dust removal device and its use method
CN101757844B (en) * 2008-12-24 2013-12-04 中石化宁波工程有限公司 Method and device for performing flue gas desulfurization by using ammonia process
CN101837235B (en) * 2009-03-19 2012-08-29 北京九州美电科技有限公司 Low-consumption high-efficiency boiler flue gas desulfurization process
CN101601964B (en) * 2009-06-03 2012-01-11 李鹏举 Ammonia flue gas desulfurization device
CN101670231B (en) * 2009-07-23 2011-08-24 何金整 Device and process for converting calcium process desulfurization into temperature difference crystallizing ammonia process desulfurization
CN101780368A (en) * 2010-03-26 2010-07-21 张蕊 Low energy consumption flue gas wet desulphurization process
CN101844034A (en) * 2010-06-18 2010-09-29 宁波金远东工业科技有限公司 Device for removing sulfur dioxide from waste gas and producing ammonium sulfate byproduct
CN101844034B (en) * 2010-06-18 2012-11-21 宁波金远东工业科技有限公司 Device for removing sulfur dioxide from waste gas and producing ammonium sulfate byproduct
CN102847422B (en) * 2011-07-22 2015-06-17 上海克硫环保科技股份有限公司 Apparatus for desulfurizing smoke through ammonia process
CN102847422A (en) * 2011-07-22 2013-01-02 上海克硫环保科技股份有限公司 Apparatus for desulfurizing smoke through ammonia process
CN102850092A (en) * 2011-08-31 2013-01-02 上海克硫环保科技股份有限公司 Technology for producing ammonium sulfate fertilizer through desulfurizing smoke by ammonia process, and apparatus thereof
CN102559959A (en) * 2012-03-13 2012-07-11 武汉宜生机电技术工程有限公司 Blast furnace water granulated slag steam desulfuration and water recycling device
CN102559959B (en) * 2012-03-13 2014-04-09 武汉宜生机电技术工程有限公司 Blast furnace water granulated slag steam desulfuration and water recycling device
CN103263841A (en) * 2013-05-27 2013-08-28 史永军 Method for removing aerosol in ammonia washing desulphurization of flue gas
CN105311937A (en) * 2014-06-11 2016-02-10 成都新筑展博环保科技有限公司 Method of producing ammonium sulfate through flue gas desulfurization
CN104368223A (en) * 2014-11-07 2015-02-25 广德瑞邦涂料有限公司 Waste gas absorption device for synthesizing anodic electrophoretic paint resin
CN104482778A (en) * 2014-12-12 2015-04-01 湖南科技大学 Device and method for treating and using fume waste heat during harmful tail gas treatment
CN105854562A (en) * 2016-05-14 2016-08-17 张波 Ultralow-emission desulfurization absorption device
CN106823740A (en) * 2017-01-23 2017-06-13 上海大学 Charcoal element stove, the ammonia process of desulfurization of coke oven flue gas multisection type and dedusting absorption tower
CN107261789A (en) * 2017-06-15 2017-10-20 上海交通大学 The ammonia method desulfurizing system and method for a kind of high-sulfur flue gas

Similar Documents

Publication Publication Date Title
CN101579602B (en) Energy-saving and high-quality ammonia desulphurization process for ammonia sulfate recovery
CN101422691B (en) Multi-pollutant removing technique and device of fuel coal smoke
CN106659971A (en) Method and apparatus for removing contaminants from exhaust gases
CN100496675C (en) Simultaneous desulfurization and denitration wet ammonia flue gas cleaning technology and system thereof
CN100435910C (en) Fume desulfurizing process employing multiple circulation and stable double alkali method and apparatus
CN203507793U (en) Device for simultaneously removing sulfur dioxide and nitrogen oxide from coke oven flue gas
CN103303872B (en) System device and method for recycling sulfur dioxide from fume to prepare sulfur
US5674459A (en) Hydrogen peroxide for flue gas desulfurization
CN201380037Y (en) Flue-gas cleaner with functions of desulphurization, denitration, concentration and crystal
CN103303877B (en) Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process
RU2459655C2 (en) Device and method of smoke fumes
CN100490946C (en) Sintering flue gas ammonia method desulfurizing system
CN101343077B (en) Method for preparing gypsum by removing boiler flue gas sulphur dioxide with white slime from ammonia alkali factory
CN101637685B (en) Comprehensive treatment method of sulfur-containing flue gas
CN100364647C (en) Ammonia type flue gas desulfurizing apparatus and its process
CN102423613B (en) Ammonia desulfurization method for effectively removing chlorine and fluorine ions and heavy metal ions
CN103868087B (en) A kind of collaborative enhancing PM2.5The method of elimination and fume afterheat deep exploitation and device
CN101524620B (en) Segment-based ammonia method flue gas desulfurization device
CN1408464A (en) Removing and recovering process and device for SO2 in flue gas
CN201880482U (en) Stepped spray tower for desulfurization by ammonia method
CN103041678B (en) Ammonia flue gas desulfuration and denitration combined process and device
CS203105B2 (en) Method of removing the sulphur dioxide and other acidic components from the combustion products
CN100551494C (en) Ammonia process removes the method and the system thereof of carbon dioxide in the generating plant flue gas
CN100460045C (en) Process for disposing SOx in discharge gas
CN100558448C (en) The operation method of flue gas desulfurization equipment and exhaust gas desulfurization equipment and flue gas desulfurization equipment

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
C17 Cessation of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20080102

Termination date: 20110209