CN201092536Y - Ammonium sulfate production equipment having air distribution component - Google Patents
Ammonium sulfate production equipment having air distribution component Download PDFInfo
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- CN201092536Y CN201092536Y CNU2007201512619U CN200720151261U CN201092536Y CN 201092536 Y CN201092536 Y CN 201092536Y CN U2007201512619 U CNU2007201512619 U CN U2007201512619U CN 200720151261 U CN200720151261 U CN 200720151261U CN 201092536 Y CN201092536 Y CN 201092536Y
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- tower body
- oxidation air
- sulphur ammonium
- production unit
- absorption
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Abstract
The utility model relates to a device for producing ammonium sulfate, in particular to a device with an air distribution component for producing ammonium sulfate, which comprises a tower body, a washing absorption segment and an oxide crystallization segment, wherein the washing absorption segment is arranged on the upper portion of the tower body and the oxide crystallization segment is arranged on the lower portion of the washing absorption segment. The oxide crystallization segment comprises an overflowing output of absorption liquid, an oxidation air input, an absorption recycle liquid output, a slurry reflux input for dehydration of the ammonium sulfate, an ammonia sulfate slurry output, a stirring device and an oxidation air distributed component, wherein the absorption liquid overflow output is arranged on the upper portion of the oxide crystallization segment, the oxidation air input is arranged on the lower portion of the absorption liquid overflowing output, the absorption recycle liquid output is arranged on the lower portion of the oxidation air input, and the slurry reflux input for dehydration of the ammonium sulfate is arranged on the upper portion of the oxidation air input. The ammonia sulfate slurry output is arranged on the lower portion of the absorption recycle liquid output, the stirring device is arranged between the absorption liquid overflowing output and the bottom of the tower body, and the oxidation air distributed component which is arranged in the tower body and is close to the stirring device is connected with the oxidation air input. The device of the utility model forms an optimization design for an entering form of the air, thereby increasing the mass transfer rate and the oxidation results of oxygen and the efficiency of the device.
Description
Technical field
The utility model relates to a kind of equipment of producing the sulphur ammonium, is specifically related to the oxidizing and crystallizing section of equipment.
Background technology
With coal or oil is that a large amount of flue gases are discharged in the boiler or the fuel-burning power plant of fuel.These flue gases contain objectionable impuritiess such as SOx, NOx, HCl and HF, and wherein SOx is the essential substance that forms acid rain.With the difference of burning coal, SO
2Content is usually at 300-5000ppmv (1000-15000mg/Nm
3) between.But exhaust gas volumn is very huge, and the opinion with coal firing boiler, steam scale are from 35T/h to 2500T/h, and generating set capacity 6MW is to 1000MW, and exhaust gas volumn is by 50,000 Nm
3/ h to 250 ten thousand Nm
3, SO
21000 tons/year to 100,000 tons/year of quantity dischargeds.Because SO
2Be sour gas, the employing alkaline aqueous solution takes off the SOx in the smoking gas, i.e. flue gas desulfurization (FGD) is effective means, is with a wide range of applications.
Synthetic ammonia is alkaline matter, as sweetening agent, can produce the ammonium sulfate fertilizer of high fertilizer efficiency.This method is called ammonia-process desulfurization technique.
China is a population, grain and chemical fertilizer big country, and the output of chemical fertilizer is converted into synthetic ammonia, is equivalent to 3,500 ten thousand tons/year.Can solve 2,000 ten thousand tons of SO with the FGD technology
2/ year calculating need provide 1,000 ten thousand tons/year of synthetic ammonia, accounts for national synthetic ammonia aggregate demand less than 30%, can produce 4,000 ten thousand tons of ammonium sulfate, nearly 30,000,000,000 yuan of the output value simultaneously.In addition, carbon ammonium or urea only contain nitrogen nutrition, and nitrogenous and sulphur nutrition simultaneously in the sulphur ammonium.Therefore, the sulphur ammonium is than carbon ammonium and the better chemical fertilizer of urea, has huge market outlook in China.But, China, so in the world wide, the output of ammonium sulfate is all very low, all is byproduct basically, does not almost have the factory that produces ammonium sulfate fertilizer specially.Therefore, development is based on the thiamine fertilizer industry of flue gas desulfurization, for promoting that China's Agricultural Development is significant.
Three steps of ammonia-process desulfurization technique correspondence are as follows:
(1) SO
2Absorb, show as the acid-base reaction in the aqueous solution, at first generate ammonium sulphite, react as follows:
SO
2+ H
2O+2NH
3=(NH
4)
2SO
3(ammonium sulphite)
(2) sulfite oxidation is an ammonium sulfate, and chemical reaction also takes place in the aqueous solution, reacts as follows:
(NH
4)
2SO
3+ 1/2O
2=(NH
4)
2SO
4(ammonium sulfate)
(3) ammonium sulfate crystallization after the ammonium sulfate concentrations in the aqueous solution surpasses solubleness, can crystallization be separated out the solid ammonium sulfate particle.Crystallization also is looked at as a chemical reaction usually, that is:
(NH
4)
2SO
4(L, fluid sulphuric acid ammonium)=(NH
4)
2SO
4(S, solid ammonium sulfate).
Because ammonia is soluble in water, its first step is easy to realize that assimilated efficiency is very high, can reach more than 99%.But because the more distinctive character of ammonium salt system, the sulfite oxidation in second step is an ammonium sulfate, showed a lot of singularity with the ammonium sulfate crystallization in the 3rd step, caused present industrialization technology very complicated, equipment is huge, the energy consumption height, very uneconomical, be difficult to effectively be promoted.
Sulfite oxidation is compared obvious difference with other sulphite, be that along with the continuous accumulation of ammonium sulfate concentrations in the solution, ammonium sulfate produces powerful damping action to the oxidation of ammonium sulphite, promptly along with the increase of sulphur ammonium concentration, the oxidation rate of ammonium sulphite sharply reduces.Prior art can significantly hinder O from ammonium sulfate
2This angle of dissolving in the aqueous solution has been set forth this peculiar property.When salt concn during less than 0.5mol/L (about 5% (wt)), the ammonium sulfurous rate of oxidation increases with its concentration, and when surpassing this ultimate value, rate of oxidation increases with concentration and reduces.
Though the oxidation of ammonium sulphite outwardly with SO
2Absorption it doesn't matter, still,, will suppress SO conversely if sulfite oxidation is insufficient
2Absorption.Therefore, with other sulfur methods, such as the calcium method that with the Wingdale is raw material different with the magnesium method that with magnesium oxide is raw material be the oxidising process of ammonia process and SO
2Absorption process is of equal importance.In calcium method and magnesium method, SO
2Assimilated efficiency almost irrelevant with the oxidising process of sulphite (calcium sulfite and magnesium sulfite).Why will emphasize oxidation in these two kinds of methods, especially limestone-gypsum methods, be because will prevent the thionizer fouling stops up, and after wishing to be translated into gypsum, desulfuration byproduct can obtain utilizing.This yet early stage just calcium method does not have the reason of oxidized portion.
For this reason, both at home and abroad industry member released a kind of multi-functional be the flue gas desulfurization (FGD) unit of raw material with ammonia, ammonium sulfurous oxidation and sulphur crystalline ammonium are separately carried out, guaranteed that the ammonium sulfate concentrations of oxidation panel (in the bottom, absorption tower) is controlled at lower level, improve oxidation rate.Between oxidation panel (being positioned at the bottom) and absorber portion, be provided with enriching section dexterously.Although this technology has been utilized the characteristics of sulfite oxidation preferably, thionizer is slightly existing complicated, and cost is higher, and in addition, flow process is also longer.
Its major cause is, the realization of prior art is based on the intrinsic reaction kinetics of sulfite oxidation process.Obviously, the oxidation effectiveness of sulphite be improved, the rate of mass transfer of oxygen must be strengthened and improve.
Summary of the invention
The utility model technical issues that need to address are to disclose a kind of sulphur ammonium production unit with air distribution member, to overcome the above-mentioned defective that prior art exists.
Sulphur ammonium production unit with air distribution member of the present utility model comprises:
Tower body;
Be arranged on the washing absorber portion on said tower body top;
The oxidizing and crystallizing section that fuses with the washing absorber portion that is arranged on washing absorber portion below;
Said washing absorber portion is a prior art, and the utility model repeats no more;
Said oxidizing and crystallizing section comprises:
Be arranged on the absorption liquid overflow outlet on the tower body of oxidizing and crystallizing section top, be used for the liquid level of crystallization control section;
Be arranged on the oxidation air inlet on the tower body of overflow outlet below;
Be arranged on the absorption circulation fluid outlet on the tower body of oxidation air inlet below;
Be arranged on the slurry reflux inlet of the sulphur ammonium dehydration on the tower body of oxidation air inlet top;
Be arranged on the ammonium sulfate slurry outlet on the tower body that absorbs circulation fluid outlet below;
1～6 layer of whipping appts between being arranged at the bottom of overflow outlet and the tower;
It is characterized in that, also comprise be connected with oxidation air inlet be arranged on tower intravital, near the oxidation air distributed component of whipping appts.
The utility model is operation like this:
Contain SO
2Flue gas the washing absorber portion contact with absorption liquid, generate ammonium sulphite, enter the oxidizing and crystallizing section of the thionizer bottom of the ammonia process of desulfurization, air enters in the tower body from the oxidation air inlet, discharge by said distribution pipe, being stirred device earlier disperses, then further by uniform distribution, contact with ammonium sulphite, be oxidized to ammonium sulfate, and form crystallization, the slip that contains ammonium sulfate crystallization is sent to follow-up dehydration workshop section from the ammonium sulfate slurry outlet, preparing product, absorption liquid flows out from absorbing the circulation fluid outlet, recycles once more.
Sulphur ammonium production unit with air distribution member of the present utility model, fully take into account oxygenant, the mass transfer process that is oxygen is the key factor of the whole oxidising process of restriction, therefore, the enter mode of air has been made optimization design, by whipping appts and oxidation air distributed component, air is disperseed and uniform distribution, improve the rate of mass transfer of oxygen, improved the oxidation effectiveness of sulphite greatly, thereby improved the efficient of equipment.
Description of drawings
Fig. 1 is the sulphur ammonium production unit structural representation with air distribution member.
To be whipping appts, oxidation air distributed component cooperate synoptic diagram with tower body amplifies to Fig. 2.
Embodiment
Referring to Fig. 1, the sulphur ammonium production unit with air distribution member of the present utility model comprises:
Be arranged on the washing absorber portion 20 on said tower body 1 top;
The oxidizing and crystallizing section 30 that fuses with washing absorber portion 20 that is arranged on washing absorber portion 20 belows;
Said washing absorber portion 20 comprises:
Be arranged on the first exhaust gases passes mouth 2 at tower body 1 top;
Be arranged on the circulation fluid inlet 3 on the tower body 1 of the first exhaust gases passes mouth, 2 belows;
Be provided with the said first exhaust gases passes mouth 2 belows, with circulation fluid inlet 3 recycle liquid distributors that are connected 31;
Be arranged on the second exhaust gases passes mouth 4 on the tower body 1 of said recycle liquid distributor 3 belows;
Said oxidizing and crystallizing section 30 comprises:
Be arranged on the absorption liquid overflow outlet 5 on the tower body 1 on oxidizing and crystallizing section 30 tops, be used for the liquid level of crystallization control section;
Be arranged on the oxidation air inlet 6 on the tower body 1 that the absorption liquid overflow exports 5 belows;
Be arranged on enter the mouth absorption circulation fluid outlet 7 on the tower body 1 of 6 belows of oxidation air;
Be arranged on the slurry reflux inlet of the sulphur ammonium dehydration on the tower body of oxidation air inlet top;
Be arranged on the ammonium sulfate slurry outlet 8 that absorbs on the tower body 1 that circulation fluid exports 7 belows;
1～6 layer of whipping appts 9 between being arranged at the bottom of absorption liquid overflow outlet 5 and the tower;
It is characterized in that, also comprise be connected with oxidation air inlet 6 be arranged in the tower body 1, near the oxidation air distributed component 601 of whipping appts 9;
Referring to Fig. 2, said oxidation air distributed component comprises straight tube 10 and arm 11, one end of straight tube 10 is connected with oxidation air inlet 6, the other end of straight tube 10 is connected with an end of arm 11, the other end 12 and the level interval L between the whipping appts 9 of arm 11 are 0.2～2.0m, and the other end 12 and the vertical spacing H between the whipping appts 9 of arm 11 are 0.1～1.0m;
Further, the other end 12 of arm 11 is provided with groove, so that the dispersion of air, groove face is to the axis of tower body 1, and the angle γ of groove is 10～80 °; The groove angle γ that optimizes is 20～60 °;
Said oxidation air inlet 6 can be arranged on the top of whipping appts 9, also can be arranged on the below of whipping appts 9;
Referring to Fig. 1 and Fig. 2, said whipping appts 9 comprises stir shaft 901 and is fixed on the agitating vane 902 of stir shaft 901 ends that said stir shaft 901 passes the tower wall of said tower body 1, with actuating unit, be connected as motor, be provided with containment member between stir shaft 901 and the tower body 1;
Said whipping appts 9 preferred 2～4 layers, every layer is provided with 1～6 whipping appts 9, preferred 2～4;
Further, the whipping appts 9 of the lowest layer, the main solid suspension that plays a part, the distance of itself and tower body 1 bottom is 1-2m, the whipping appts 9 of lowest layer whipping appts 9 tops and the distance between the lowest layer whipping appts 9, and the distance between other each layer whipping appts 9 is 3-6 times of agitating vane 902 diameters.
Claims (10)
1. an ammonia process sulphur ammonium production unit is characterized in that, said sulphur ammonium production unit comprises:
Thionizer tower body (1);
Be connected with oxidation air inlet (6), be arranged on tower body (1) inside, near the oxidation air distributed component (601) of whipping appts (9).
2. ammonia process sulphur ammonium production unit according to claim 1 is characterized in that, said sulphur ammonium production unit also comprises:
Be arranged on the washing absorber portion (20) on said tower body (1) top;
Be arranged on washing absorber portion (20) below with the oxidizing and crystallizing section (30) that fuses of washing absorber portion (20).
3. ammonia process sulphur ammonium production unit according to claim 2 is characterized in that said oxidizing and crystallizing section (30) comprising:
Be arranged on the absorption liquid overflow outlet (5) on the tower body (1) on oxidizing and crystallizing section (30) top;
Be arranged on the oxidation air inlet (6) on the tower body (1) of absorption liquid overflow outlet (5) below;
Be arranged on the absorption circulation fluid outlet (7) on the tower body (1) of oxidation air inlet (6) below;
Be arranged on the slurry reflux inlet of the sulphur ammonium dehydration on the tower body of oxidation air inlet top;
Be arranged on the ammonium sulfate slurry outlet (8) on the tower body (1) that absorbs circulation fluid outlet (7) below;
1～6 layer of whipping appts (9) between being arranged at the bottom of absorption liquid overflow outlet (5) and the tower.
4. according to each described ammonia process sulphur ammonium production unit of claim 1 to 3, it is characterized in that, said oxidation air distributed component (601) comprises straight tube (10) and arm (11), one end of straight tube (10) is connected with oxidation air inlet (6), the other end of straight tube (10) is connected with an end of arm (11), and the other end (12) of arm (11) and the level interval L between the whipping appts (9) are 0.1～2.0m.
5. ammonia process sulphur ammonium production unit according to claim 4 is characterized in that, the other end (12) of arm (11) and the vertical spacing H between the whipping appts (9) are 0.1～1.0m.
6. according to claim 4 or 5 described ammonia process sulphur ammonium production units, it is characterized in that the other end (12) of arm (11) is provided with groove, groove face is to the axis of tower body (1).
7. ammonia process sulphur ammonium production unit according to claim 6 is characterized in that the angle γ of groove is 10～80 °.
8. according to each described ammonia process sulphur ammonium production unit of claim 1 to 7, it is characterized in that said oxidation air inlet (6) is arranged on the optional position, top of whipping appts (9).
9. according to each described ammonia process sulphur ammonium production unit of claim 1 to 7, it is characterized in that said oxidation air inlet (6) is arranged on the optional position, bottom of whipping appts (9).
10. according to each described ammonia process sulphur ammonium production unit of claim 1 to 7, it is characterized in that said oxidation air inlet (6) is arranged on and the parallel optional position of whipping appts (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201512619U CN201092536Y (en) | 2007-06-11 | 2007-06-11 | Ammonium sulfate production equipment having air distribution component |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201512619U CN201092536Y (en) | 2007-06-11 | 2007-06-11 | Ammonium sulfate production equipment having air distribution component |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201092536Y true CN201092536Y (en) | 2008-07-30 |
Family
ID=39900500
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007201512619U Expired - Fee Related CN201092536Y (en) | 2007-06-11 | 2007-06-11 | Ammonium sulfate production equipment having air distribution component |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201092536Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103936032A (en) * | 2014-04-08 | 2014-07-23 | 攀钢集团西昌钢钒有限公司 | Method for producing large granular ammonium sulfate product |
| CN108285154A (en) * | 2017-12-29 | 2018-07-17 | 攀钢集团西昌钢钒有限公司 | Precipitation ammonium sulfate device for making |
-
2007
- 2007-06-11 CN CNU2007201512619U patent/CN201092536Y/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103936032A (en) * | 2014-04-08 | 2014-07-23 | 攀钢集团西昌钢钒有限公司 | Method for producing large granular ammonium sulfate product |
| CN103936032B (en) * | 2014-04-08 | 2016-02-03 | 攀钢集团西昌钢钒有限公司 | A kind of production method of large-particle ammonium sulfate product |
| CN108285154A (en) * | 2017-12-29 | 2018-07-17 | 攀钢集团西昌钢钒有限公司 | Precipitation ammonium sulfate device for making |
| CN108285154B (en) * | 2017-12-29 | 2021-08-17 | 攀钢集团西昌钢钒有限公司 | Device is prepared to heavy vanadium ammonium sulfate |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Shenchuan Environment Protection Science and Technology Co., Ltd., Shanghai Assignor: Lou Aijuan Contract fulfillment period: 2009.2.8 to 2011.2.8 Contract record no.: 2009310000011 Denomination of utility model: Ammonium sulfate production equipment having air distribution component Granted publication date: 20080730 License type: Exclusive license Record date: 20090225 |
|
| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.2.8 TO 2011.2.8; CHANGE OF CONTRACT Name of requester: SHENCHUAN ENVIRONMENT PROTECTION TECH CO., LTD., S Effective date: 20090225 |
|
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Shenchuan Environment Protection Science and Technology Co., Ltd., Shanghai Assignor: Lou Aijuan Contract fulfillment period: 2009.4.9 to 2016.4.9 Contract record no.: 2009310000102 Denomination of utility model: Ammonium sulfate production equipment having air distribution component Granted publication date: 20080730 License type: Exclusive license Record date: 20090619 |
|
| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.4.9 TO 2016.4.9; CHANGE OF CONTRACT Name of requester: SHENCHUAN ENVIRONMENT PROTECTION TECH CO., LTD., S Effective date: 20090619 |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080730 Termination date: 20140611 |