CN102976359A - Method for producing ammonium sulfate by removing sulfur through ammonia method - Google Patents
Method for producing ammonium sulfate by removing sulfur through ammonia method Download PDFInfo
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- CN102976359A CN102976359A CN2012105603190A CN201210560319A CN102976359A CN 102976359 A CN102976359 A CN 102976359A CN 2012105603190 A CN2012105603190 A CN 2012105603190A CN 201210560319 A CN201210560319 A CN 201210560319A CN 102976359 A CN102976359 A CN 102976359A
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Abstract
The invention discloses a sulfur removal technology belonging to air pollution regulation, and particularly relates to a method for producing ammonium sulfate by removing sulfur through an ammonia method. The method comprises the following steps: introducing ammonia water and tail gas containing sulfur dioxide into a tail gas treatment tower, reacting the sulfur dioxide in the exhaust with the ammonia water to remove sulfur, defogging the gas subjected to sulfur removal, then discharging to obtain a circulating absorption liquid in the tail gas treatment tower, and controlling the pH value of the circulating absorption liquid at 5-6 and the temperature at 40-45 DEG C; concentrating the circulating absorption liquid with tail gas containing sulfur dioxide, which is generated in sulfuric acid production; and when the density is 1.18-1.22 g/cm<3>, partially taking out to prepare solid ammonium sulfate or prepare a 30-40% (mass percentage concentration) ammonium sulfate liquid, and simultaneously recovering the generated sulfur dioxide gas. Thus, the method disclosed by the invention overcomes the problems that ammonium sulfite generated by treating sulfur dioxide through the common ammonia method is low in concentration and high-concentration ammonium sulfite is difficult to oxidize, realizes the low-cost operation of sulfuric acid tail gas treatment, and achieves the purposes of treating one waste with another waste and preparing the waste into a fertilizer.
Description
Technical field
The present invention relates to a kind of improvement desulfurization technology of topsoil, particularly the method for ammonium sulfate is produced in a kind of ammonia process of desulfurization.
Background technology
The tail gas that the industrial sulphuric acid device is discharged is the environmental issue of global concern, and its sulfurous gas must be processed, qualified discharge.Along with country is increasingly strict to environmental requirement, on October 1st, 2013, the new sulfuric acid industry pollutant emission standard of country will formally be implemented, and the tail gas sulphur dioxide discharge index of new standard regulation is 400mg/Nm
3, have at present a lot of old gas washing in SA production factories also to fail to reach this index.
In the existing desulfurization technology, the desulfuration efficiency of ammonia type flue gas desulfurizing method is higher.Ammonia type flue gas desulfurizing mainly comprises: sulfur-containing tail gas reclaims with ammoniacal liquor and further oxidation and the utilization of byproduct ammonium sulphite.The product that the ammonia type flue gas desulfurizing method reclaims sulfurous gas is mainly ammonium sulphite, sulfur dioxide liquid, ammonium sulfate liquor, high density ammonium bisulfite etc.Although ammonium sulphite also can be used as chemical fertilizer and directly uses, the less stable of product, difficulty is accepted by the peasant; Such as the raw materials for production as little paper mill, will produce waste water, cause secondary pollution.If with ammonium sulphite direct oxidation production high-quality ammonium sulfate fertilizer, although be more satisfactory sulfuric acid tail gas processing mode, but at present employing directly passes into air and sulfite oxidation is produced the ammonium sulfate method has following problem: (1) oxidation efficiency is lower: the oxidation ratio of the ammonium sulphite when concentration is 10% left and right sides is about 90%, and the oxidation ratio of the ammonium sulphite when concentration is 30% left and right sides only has about 60%; (2) need to add catalyzer in the oxidising process and catalyzer is expensive; (3) coefficient of oxygen utilization is low during oxidation, and power consumption is large, and the Effects Analysis cost is high; Higher oxidation ratio is only just arranged when low concentration when (4) being direct oxidation into ammonium sulfate owing to ammonium sulphite, cause the ammonium sulfate concentrations in the circulating absorption solution also very low, when generating ammonium sulfate, processing needs a large amount of outer by force evaporating, concentrating and crystallizings of steam that supplies, energy consumption is large, equipment corrosion is tight, flow process is complicated, and investment is high, and the automated operation level is low; Have discharge of wastewater when (5) ammonium sulphite is direct oxidation into ammonium sulfate, sweetening agent ammoniacal liquor consumption is large, carries a large amount of free ammonias during exhaust emissions secretly, and the ammonia loss causes greatly and easily secondary pollution problems.Ammonia Production factory whenever has a large amount of deposed ammonias to discharge every year simultaneously, and how reasonable, economic this deposed ammonia that utilizes also is the difficult problem of Ammonia Production factory.
Summary of the invention
The object of the invention is to overcome existing above-mentioned deficiency in the prior art, provide a kind of ammonia process of desulfurization to produce the method for ammonium sulfate.The method is not added any catalyst decomposes ammonium sulphite, and the ammonium sulfate concentrations that obtains is high, and power consumption is low, and desulfuration efficiency is high.
In order to realize the foregoing invention purpose, the invention provides following technical scheme:
(1) ammoniacal liquor and the tail gas that contains sulfurous gas are passed into the vent gas treatment tower, sulfurous gas in the tail gas and ammoniacal liquor carry out reaction desulfuration, then gas after the desulfurization discharge through demist, obtain circulating absorption solution in the vent gas treatment tower, the pH value of controlled circulation absorption liquid is 5～6, temperature is 40～45 ℃;
(2) tail gas that contains sulfurous gas of circulating absorption solution through producing the sulfuric acid generation that obtains when step () concentrates, and density reaches 1.18～1.22g/cm
3The time, the part circulating absorption solution is shifted out the vent gas treatment tower;
(3) in remaining circulating absorption solution, continue to pass into ammoniacal liquor and the tail gas that contains sulfurous gas, then repeating step (), (two);
(4) circulating absorption solution that step (two) is shifted out from the vent gas treatment tower decomposes with sulphur trioxide or sulfuric acid, obtains ammoniumsulphate soln and sulfur dioxide gas, with described ammoniumsulphate soln concentrate, Crystallization Separation obtains solid ammonium sulfate;
(5) sulfurous gas that step (four) is obtained recycles.
As mentioned above, the described ammonia concn of step () is 5～20%.
As mentioned above, the described tail gas that contains sulfurous gas of step () is the tail gas that produces when producing sulfuric acid, and temperature is 60 ℃～70 ℃.
Preferably, the described demist of step () is the mist eliminator that adopts.
In the aforesaid circulating absorption solution, contain one or more in ammonium bisulfite, ammonium sulphite, the ammonium sulfate.
As mentioned above, decomposing with sulphur trioxide or sulfuric acid described in the step (four), described sulphur trioxide is gaseous state or liquid state, described sulfuric acid concentration is 93～98%, generating the mass percentage concentration that can be used as liquid fertilizer after decomposing is 30～40% ammoniumsulphate solns and sulfur dioxide gas, and described ammonium sulfate is molten to obtain the solid ammonium sulfate product after concentrated, Crystallization Separation.
Aforesaid sulfurous gas recycles, and is preferred, is described sulfurous gas to be passed into sulfuric acid production system produce sulfuric acid, or described sulfurous gas is passed into the vent gas treatment tower.
The aforesaid ammonia process of desulfurization is also applicable to the gas fitting desulfurization; The desulfurization of oil refining apparatus process; Power plant desulfurization etc.
The method of ammonium sulfate is produced in the ammonia process of desulfurization of the present invention, ammoniacal liquor and the tail gas that contains sulfurous gas are carried out desulphurization reaction in the vent gas treatment tower, the circulating absorption solution that obtains after adopting sulphur trioxide or sulfuric acid to desulphurization reaction decomposes, obtain ammonium sulfate product, the consumption of ammoniacal liquor is 0.25t/h～0.45t/h, SO in the tail gas
2Concentration be 1700mg/Nm
3～2000 mg/Nm
3, the consumption of sulphur trioxide is 0.018t/h～0.0245 t/h.
Adopting ammoniacal liquor that the tail gas that contains sulfurous gas is carried out desulfurization processes, obtain containing the circulating absorption solution of ammonium bisulfite, ammonium sulphite, ammonium sulfate in the vent gas treatment tower, ammonium sulphite has good receptivity to sulfurous gas, it is main absorber, ammonium sulphite in the middle of circulating absorption solution part in the vent gas treatment tower is oxidized to ammonium sulfate, and content is very low.Principal reaction in the tail gas absorber is as follows:
SO
2+NH
3+H
2O=NH
4HSO
3
SO
2+2NH
3+H
2O=(NH
4)
2SO
3
SO
2+(NH
4)
2SO
3+H
2O=2NH
4HSO
3
NH
3+ NH
4HSO
3=(NH
4)
2SO
3
2(NH
4)
2SO
3+O
2=2(NH
4)
2SO
4
Circulating absorption solution density in the vent gas treatment tower is 1.18～1.22g/cm
3The time, shift out the part circulating absorption solution, remove part and can be arbitrary proportion with the circulating absorption solution that remains in the vent gas treatment tower.Circulating absorption solution density is 1.18～1.22g/cm
3The time add sulphur trioxide or sulfuric acid decomposes, ammonium sulphite and sulphur trioxide or sulfuric acid can complete reactions, same ammonium bisulfite and sulphur trioxide or sulfuric acid also can complete reactions.The ammoniumsulphate soln that decomposition is obtained concentrates, the solid ammonium sulfate produced of Crystallization Separation.Also can decompose the high-concentration sulfuric acid ammonium liquid fertilizer that obtains mass percentage concentration 30～40% with adding sulphur trioxide or sulfuric acid, reach the purpose of " with the useless fertilizer of giving birth to ".The contriver finds, when density less than 1.18g/cm
3Circulating absorption solution when adding sulfuric acid and carrying out acidolysis, the mass percentage concentration of the ammoniumsulphate soln of generation is lower, is unfavorable for directly being used as liquid fertilizer, it is large to make the ammonium sulfate solids energy consumption after concentrated, crystallization, the separation; Density is greater than 1.22g/cm
3Circulating absorption solution can reduce circulating absorption solution to the specific absorption of sulfurous gas, is 1.18～1.22g/cm so select density
3Circulating absorption solution decompose.The principal reaction of decompose, concentrate, crystallizer tank is interior is as follows:
When adopting sulphur trioxide decomposition:
(NH
4)
2SO
3+ SO
3+ H
2O＝(NH
4)
2SO
4+ SO
2+H
2O
2(NH
4)HSO
3+ SO
3+ H
2O＝(NH
4)
2SO
4+ 2SO
2+2H
2O
When adopting sulfuric acid to decompose:
(NH
4)
2SO
3+ H
2SO
4＝(NH
4)
2SO
4+ SO
2+H
2O
2(NH
4)HSO
3+ H
2SO
4＝(NH
4)
2SO
4+ 2SO
2+2H
2O
The above-mentioned ammonia process of desulfurization is produced when decomposing ammonium sulphite in the method for ammonium sulfate, does not add any catalyzer, has saved cost, power consumption is low.Desulfurization degree can reach more than 95%, SO in the gas of discharging
2Concentration≤95mg/Nm
3
Further, the above-mentioned ammonia process of desulfurization is produced in the method for ammonium sulfate, and it is the ammoniacal liquor of 5-7% that ammoniacal liquor can adopt the concentration of the ammonia that produces in the production of synthetic ammonia, can reach the purpose of " waste recycling ".If select ammonia concentration less than 5% ammoniacal liquor, the mass percentage concentration of the ammoniumsulphate soln for preparing after the ammonia process of desulfurization is less than 30%; If select ammonia concentration greater than 20% ammoniacal liquor, the escape amount of the gaseous ammonia after the desulfurization is greater than 10mg/Nm
3
The above-mentioned ammonia process of desulfurization is produced in the method for ammonium sulfate, then gas demist after adopting mist eliminator to desulfurization discharges, remove the droplet of carrying secretly in the gas, can reduce water content, reduce as far as possible the concentration of " aerosol " in the tail gas, and the escape of establishment gas phase free ammonia, the escape amount of ammonia≤8 mg/Nm
3
The tail gas that contains sulfurous gas of producing the sulfuric acid generation belongs to over dry tail gas, and its temperature reaches 60 ℃～70 ℃, utilizes its waste heat that circulating absorption solution is concentrated, and can further reduce energy consumption.
The sulfurous gas that decomposition is obtained passes into sulfuric acid production system and produces sulfuric acid or pass into the vent gas treatment tower and recycle, realizes non-pollution discharge.
Compared with prior art, beneficial effect of the present invention:
The present invention utilizes ammoniacal liquor, can be the deposed ammonia that synthetic ammonia produces, and the sulfurous gas in the sulfuric acid tail gas is administered, and desulfuration efficiency is high, generally greater than 95%, and SO in the gas after the processing
2Concentration is minimum≤95mg/Nm
3, effectively realizing the sulfurous gas qualified discharge.When decomposing ammonium sulphite, do not add any catalyzer, just can obtain mass percentage concentration is that 30～40% ammoniumsulphate solns can be used as liquid fertilizer, with described ammoniumsulphate soln concentrate, the Crystallization Separation technology makes ammonium sulfate solids fertilizer.Concentration is that 30～40% ammonium sulfite solutions also can be directly as liquid fertilizer.Overcome the low and dysoxidizable difficult problem of high density ammonium sulphite of ammonium sulphite concentration of common ammonia process processing sulfurous gas generation, realized sulfuric acid tail gas processing low cost movement, reached the purpose of " treatment of wastes with processes of wastes against one another, living fertile to give up ".
Description of drawings:
Fig. 1 is the schema that ammonium sulfate is produced in embodiment 1 ammonia process of desulfurization.
Embodiment
The present invention is described in further detail below in conjunction with test example and embodiment.But this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment, all technology that realizes based on content of the present invention all belong to scope of the present invention.
Embodiment 1
The method of ammonium sulfate is produced in a kind of ammonia process of desulfurization, and schema may further comprise the steps as shown in Figure 1:
(1), be that 17.8% ammoniacal liquor is sent into the ammoniacal liquor header tank with recycle pump with ammonia concentration in the tank used for storing ammonia, then be that 17.8% deposed ammonia passes into the vent gas treatment tower with ammonia concentration in the ammoniacal liquor header tank, the consumption of ammoniacal liquor is 0.18t/h; The tail gas that will produce in the time of will producing sulfuric acid simultaneously, the concentration of SO2 is 1700mg/Nm3 in the tail gas, passes into the vent gas treatment tower, after the sulfurous gas in the tail gas and ammoniacal liquor carry out reaction desulfuration, SO in the tail gas
2Specific absorption is 95.06%, with discharging SO in the tail gas of discharging after the mist eliminator demist
2Concentration be down to 84mg/Nm
3, NH
3Concentration be 6.14mg/Nm
3, obtaining containing the circulating absorption solution of ammonium bisulfite, ammonium sulphite, ammonium sulfate in the vent gas treatment tower, the pH value is controlled at 5.5～5.8, temperature is 40～45 ℃, circulates with recycle pump;
(2) tail gas that contains sulfurous gas of circulating absorption solution through producing the sulfuric acid generation that obtains when step () concentrates, and density reaches 1.21g/cm
3The time, the liquid level of circulating absorption solution is 2 meters in the control absorption tower, is higher than liquid level and partly shifts out;
(3) in remaining circulating absorption solution, continue to pass into ammoniacal liquor and the tail gas that contains sulfurous gas, then repeating step (), (two) (three);
(4) circulating absorption solution that step (two) is shifted out from the vent gas treatment tower is decomposing, is being that 8% sulfur trioxide gas decomposes with concentration in concentrated, the crystallizer, the consumption of pure sulfur trioxide gas is 0.022t/h, not adding any catalyzer decomposes,, per hour obtain 0.342 ton of mass percentage concentration and be 37.6% ammoniumsulphate soln and sulfur dioxide gas; Ammoniumsulphate soln concentrates, make ammonium sulfate solids after the Crystallization Separation;
(5) sulfurous gas that step (four) is obtained passes into sulfuric acid production system with blower fan and produces sulfuric acid.
Embodiment 2
The method of ammonium sulfate is produced in a kind of ammonia process of desulfurization, may further comprise the steps:
(1), be that 13.3% deposed ammonia is sent into the ammoniacal liquor header tank with blower fan with ammonia concentration in the tank used for storing ammonia, then be that 13.3% deposed ammonia passes into the vent gas treatment tower with ammonia concentration in the ammoniacal liquor header tank, the consumption of deposed ammonia is 0.261t/h; SO in the tail gas that will produce in the time of will producing sulfuric acid simultaneously
2Concentration be 1920mg/Nm
3, tail gas passes into the vent gas treatment tower, after the desulfurization of tail gas process, and SO in the tail gas
2Specific absorption is 95.05%, with discharging SO in the tail gas of discharging after the mist eliminator demist
2Concentration 95mg/Nm
3, NH
3Concentration be 2.14mg/Nm
3, obtaining containing the circulating absorption solution of ammonium bisulfite, ammonium sulphite, ammonium sulfate, the pH value of controlled circulation absorption liquid is 5.2～5.5, temperature is 40～45 ℃, circulates with recycle pump;
(2) tail gas that contains sulfurous gas that the circulating absorption solution that obtains when step () produces through producing sulfuric acid, density reaches 1.2g/cm
3The time, the liquid level of absorption liquid is 2 meters in the control absorption tower, is higher than liquid level and partly shifts out;
(3) in remaining circulating absorption solution, continue to pass into ammoniacal liquor and the tail gas that contains sulfurous gas, then repeating step (), (two);
(4) circulating absorption solution that step (two) is shifted out from the vent gas treatment tower is that 95% sulfuric acid carries out acidolysis with concentration in the acidolysis groove, not adding any catalyzer decomposes, the consumption of sulfuric acid is 0.018t/h, per hour obtain 0.357 ton of mass percentage concentration and be 35.1% obtain ammoniumsulphate soln and sulfur dioxide gas, ammoniumsulphate soln concentrates, make ammonium sulfate solids after the crystallization, separation;
(5) sulfurous gas that step (four) is obtained passes into sulfuric acid production system with blower fan and produces sulfuric acid.
Embodiment 3
The method of ammonium sulfate is produced in a kind of ammonia process of desulfurization, may further comprise the steps:
(1), be that 7.7% deposed ammonia is sent into the ammoniacal liquor header tank with recycle pump with ammonia concentration in the tank used for storing ammonia, then be that 7.7% deposed ammonia passes into the vent gas treatment tower with ammonia concentration in the ammoniacal liquor header tank, the consumption of deposed ammonia is 0.43t/h; SO in the tail gas that will produce in the time of will producing sulfuric acid simultaneously
2Concentration be 1850mg/Nm
3, tail gas passes into the vent gas treatment tower, after the desulfurization of tail gas process, and SO in the tail gas
2Specific absorption is 95.14%, with discharging SO in the tail gas after the mist eliminator demist
2Concentration 90mg/Nm
3, NH
3Concentration be 7.52mg/Nm
3, obtaining containing the circulating absorption solution of ammonium bisulfite, ammonium sulphite, ammonium sulfate, the pH value of controlled circulation absorption liquid is 5.5～5.7, temperature is 40～45 ℃, circulates with recycle pump;
(2) tail gas that contains sulfurous gas that the circulating absorption solution that step () is obtained produces through producing sulfuric acid, density reaches 1.19g/cm
3The time, the liquid level of absorption liquid is 2 meters in the control absorption tower, is higher than liquid level and partly shifts out;
(3) in remaining circulating absorption solution, continue to pass into ammoniacal liquor and the tail gas that contains sulfurous gas, then repeating step (), (two);
(4) circulating absorption solution that step (two) is shifted out from the vent gas treatment tower is that 93% sulfuric acid carries out acidolysis with concentration in the acidolysis groove, not adding any catalyzer decomposes, the consumption of sulfuric acid is 0.015t/h, per hour obtain 0.362 ton of mass percentage concentration and be 34.6% ammoniumsulphate soln and sulfur dioxide gas, ammoniumsulphate soln concentrates, make ammonium sulfate solids after the crystallization, separation;
(5) sulfurous gas that step (four) is obtained passes into sulfuric acid production system with blower fan and produces sulfuric acid.
Claims (9)
1. the method that ammonium sulfate is produced in the ammonia process of desulfurization is characterized in that, may further comprise the steps:
(1) ammoniacal liquor and the tail gas that contains sulfurous gas are passed into the vent gas treatment tower, sulfurous gas in the tail gas and ammoniacal liquor carry out reaction desulfuration, then gas after the desulfurization discharge through demist, obtain circulating absorption solution in the vent gas treatment tower, the pH value of controlled circulation absorption liquid is 5～6, temperature is 40～45 ℃;
(2) tail gas that contains sulfurous gas of circulating absorption solution through producing the sulfuric acid generation that obtains when step () concentrates, and density reaches 1.18～1.22g/cm
3The time, the part circulating absorption solution is shifted out the vent gas treatment tower;
(3) in remaining circulating absorption solution, continue to pass into ammoniacal liquor and the tail gas that contains sulfurous gas, then repeating step (), (two);
(4) circulating absorption solution that step (two) is shifted out from the vent gas treatment tower decomposes with sulphur trioxide or sulfuric acid, obtains ammoniumsulphate soln and sulfur dioxide gas, with described ammoniumsulphate soln concentrate, Crystallization Separation obtains solid ammonium sulfate;
(5) sulfurous gas that step (four) is obtained recycles.
2. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that the described ammonia concn of step () is 5～20%.
3. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that, the described tail gas that contains sulfurous gas of step () is the tail gas that produces when producing sulfuric acid, and temperature is 60 ℃～70 ℃.
4. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that, the described demist of step () is the mist eliminator that adopts.
5. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that, contains ammonium bisulfite, ammonium sulphite, ammonium sulfate in the circulating absorption solution.
6. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that decompose with sulphur trioxide or sulfuric acid described in the step (four), described sulphur trioxide is gaseous state or liquid state, and described sulfuric acid concentration is 93～98%.
7. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that, the described solid ammonium sulfate that obtains is to adopt decomposition, concentrated, Crystallization Separation integration apparatus.
8. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that described ammoniumsulphate soln mass percentage concentration is 30-40%, can be used as liquid fertilizer.
9. the method for ammonium sulfate is produced in the ammonia process of desulfurization as claimed in claim 1, it is characterized in that, sulfurous gas described in the step (five) recycles, and is described sulfurous gas to be passed into sulfuric acid production system production sulfuric acid or passes into the vent gas treatment tower recycle again.
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| CN104512909A (en) * | 2013-09-28 | 2015-04-15 | 沈阳铝镁设计研究院有限公司 | Method and device for recovery of ammonium sulfate from sintering tail gas |
| CN104524941A (en) * | 2014-12-08 | 2015-04-22 | 中国石油集团东北炼化工程有限公司吉林设计院 | Method of absorbing tail gas containing ethylene oxide |
| CN104941404A (en) * | 2015-06-10 | 2015-09-30 | 云南驰宏锌锗股份有限公司 | Deep tail gas purification method for fuming furnace |
| CN110115919A (en) * | 2019-04-19 | 2019-08-13 | 陕西陕化煤化工集团有限公司 | It is a kind of for sulfur recovery when acid tail gas in sulphur recovery process |
| CN111573695A (en) * | 2020-04-09 | 2020-08-25 | 浙江省天正设计工程有限公司 | Recycling treatment process for high-concentration organic wastewater containing phosphorus and sulfur |
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| CN101723411A (en) * | 2009-12-18 | 2010-06-09 | 聊城鲁西化工第五化肥厂 | Process and equipment for producing potassium sulfate compound fertilizer by integrally utilizing tail gas generated in sulphuric acid production |
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| CN1600410A (en) * | 2003-09-24 | 2005-03-30 | 北京国纬达环保科技有限公司 | Integration method for ammonia process of desulfurizing flue gas and multiple utilizing desulfurized products and equipment |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104512909A (en) * | 2013-09-28 | 2015-04-15 | 沈阳铝镁设计研究院有限公司 | Method and device for recovery of ammonium sulfate from sintering tail gas |
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| CN110115919A (en) * | 2019-04-19 | 2019-08-13 | 陕西陕化煤化工集团有限公司 | It is a kind of for sulfur recovery when acid tail gas in sulphur recovery process |
| CN111573695A (en) * | 2020-04-09 | 2020-08-25 | 浙江省天正设计工程有限公司 | Recycling treatment process for high-concentration organic wastewater containing phosphorus and sulfur |
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| Publication number | Publication date |
|---|---|
| CN102976359B (en) | 2015-01-07 |
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