CN101306804A - Process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln - Google Patents
Process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln Download PDFInfo
- Publication number
- CN101306804A CN101306804A CNA2007100544119A CN200710054411A CN101306804A CN 101306804 A CN101306804 A CN 101306804A CN A2007100544119 A CNA2007100544119 A CN A2007100544119A CN 200710054411 A CN200710054411 A CN 200710054411A CN 101306804 A CN101306804 A CN 101306804A
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- CN
- China
- Prior art keywords
- flue gas
- sulfur dioxide
- concentration
- molybdenum concentrate
- gas
- Prior art date
- Legal status (The legal status 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 status listed.)
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000003546 flue gas Substances 0.000 title claims abstract description 41
- 239000002253 acid Substances 0.000 title claims abstract description 30
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 229910052750 molybdenum Inorganic materials 0.000 title claims abstract description 28
- 239000011733 molybdenum Substances 0.000 title claims abstract description 28
- 238000001354 calcination Methods 0.000 title claims abstract description 25
- 239000012141 concentrate Substances 0.000 title claims abstract description 25
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000005516 engineering process Methods 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 16
- 239000000428 dust Substances 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 230000008014 freezing Effects 0.000 claims description 3
- 238000007710 freezing Methods 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 9
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000003915 air pollution Methods 0.000 abstract 1
- 238000005406 washing Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 210000000038 chest Anatomy 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention discloses an acid production process from molybdenum concentrate calcination flue gas in a rotary kiln. The process increases sulfur dioxide concentration in molybdenum concentrate calcination flue gas from only 0.1-1.5% to 1-3% on the premise of guaranteeing product quality by using unsteady state acid production technology from low-concentration sulfur dioxide, so as to meet the thermal balance and water balance of the unsteady state acid production. The inventive process prevents the air pollution due to low-concentration sulfur dioxide, converts SO2 to sulfuric acid, and is the most economic and practical method for treating molybdenum concentrate calcination flue gas. The process has good environmental profits, as well as economic and social benefits.
Description
Technical field
The present invention relates to concentrated molybdenum ore flue gas acid preparing technical field, a kind of process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln.
Background technology
It is single thorax reflection oven process and outer heating return bend kiln mostly that domestic calcining molybdenum ore concentrate now adopts method, has only part producer to adopt the production technique of internal heating return bend kiln.Because calcining molybdenum concentrate need replenish a large amount of oxygen and the sulphur in the product could be taken off below the standard-required, therefore cause sulfur dioxide concentration in the baking flue gas generally between 0.1-1.5%.This has brought inconvenience with regard to the improvement of giving sulfur dioxide in flue gas, although domestic processing sulfurous gas adopt sodium method, calcium method and other several different methods arranged, exist expense height, dull sale, loss is big, brings problems such as secondary pollution.
Unstable state relieving haperacidity is in non-ferrous metal metallurgy industry widespread uses such as copper, lead.Because its sulfur dioxide in flue gas concentration between 2-4%, is fit to the condition of unstable state relieving haperacidity mostly.But return bend kiln calcining molybdenum concentrate sulfur dioxide in flue gas concentration has only between the 0.1-1.5%, adopts unstable state relieving haperacidity improvement sulfurous gas difficulty bigger.
Summary of the invention
The big problem of low-concentration sulfur dioxide difficulty of governance in the calcining molybdenum concentrate flue gas now provides a kind of process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln, can solve the pollution problem of low-concentration sulfur dioxide in the calcining molybdenum concentrate flue gas preferably.
In order to realize the foregoing invention purpose, the present invention adopts technical scheme as described below:
Described process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln adopts low-concentration sulfur dioxide to utilize unstable state relieving haperacidity technology, with the sulfur dioxide concentration that has only in the return bend kiln calcining molybdenum concentrate flue gas between the 0.1-1.5%; Guaranteeing that under the product quality premise, the concentration that improves the concentrated molybdenum ore sulfur dioxide in flue gas reaches between the 1-3%, satisfies the thermal equilibrium and the water balance that utilize unstable state relieving haperacidity.
The step that the dense raising of its calcining molybdenum ore concentrate flue gas acid preparing gas is taked: 1, kiln hood adds tightness system, neither allows flue gas excessive, guarantees again not advance freezing air under little negative pressure state.2, regulate direct combustion stove gas pushing quantity and induced draft fan air balance.3, control induced draft fan air quantity is able to satisfy the normal reaction air capacity.4, control the dust quantity of tornado dust collector dust discharge well, stop tornado dust collector and leak out.5, scatterer dedusting mouth adds mechanically-sealing apparatus, prevents gas leakage.6. the temperature of reaction of strict control rotary kiln.
Because adopt technique scheme, the present invention has following superiority:
This process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln is the sulfur dioxide concentration that will have only in the return bend kiln calcining molybdenum concentrate flue gas between the 0.1-1.5%, brings up between the 1-3%, adopts low-concentration sulfur dioxide to utilize unstable state relieving haperacidity technology; Can fundamentally administer low-concentration sulfur dioxide to atmospheric pollution, make SO
2Being transformed into sulfuric acid, turning waste into wealth, is the method for the most economical practicality of calcining molybdenum concentrate smoke gas treatment, not only has environmental benefit preferably, and certain economic and social benefit are arranged.
Description of drawings
Fig. 1, be return bend kiln calcining molybdenum concentrate flue gas acid preparing control chart;
Embodiment
As shown in Figure 1: this process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln needs a unstable state convertor and two reversing valves, SO in the flue gas
2Mean concns is 1.8% o'clock, and production process can realize autothermal equilibrium, does not need to open outer heating.Adopt low-concentration sulfur dioxide to utilize unstable state relieving haperacidity technology, with the sulfur dioxide concentration that has only in the return bend kiln calcining molybdenum concentrate flue gas between the 0.1-1.5%, guaranteeing under the product quality premise, the concentration that improves sulfur dioxide in flue gas reaches between the 1-3%, satisfies the thermal equilibrium and the water balance that utilize unstable state relieving haperacidity.
Low concentration SO
2The flue gas acid preparing technical process: from the flue gas of return bend kiln outlet, after the bagroom dedusting, about 100 ℃-120 ℃ of temperature, dustiness is at 2g/m
3Below enter venturi scrubber with internal injection, contact with ~ 5% dilute sulphuric acid, after adiabatic humidification washing, flue-gas temperature is reduced to about 55 ℃, most of flue dust is washed and enters in the diluted acid in the flue gas, the outlet flue gas enters stuffing washing tower, and in the diluted acid counter current contact of cat head spray, flue-gas temperature is reduced to by 55 ℃ and entered electric demist below 30 ℃ in washing tower, remove acid mist in the flue gas by electric demist, enter drying tower then, the sulfuric acid with 93% carries out drying, and dried gas is by SO
2Blower fan is delivered to the unstable state convertor and is transformed.SO after the conversion
3Gas vitriol oil with 98% in the absorption tower absorbs, and generates finished product sulfuric acid, the SO of remnants in the flue gas after the absorption
2Gas is qualified discharge after device for absorbing tail gas absorbs.The diluted acid (temperature is about 50 ℃～55 ℃) that flows out from wash tower bottoms enters the diluted acid circulation groove, send into the diluted acid plate-type heat exchanger by the diluted acid recycle pump then, behind the water coolant indirect heat exchange, diluted acid is cooled to～and 30 ℃, enter from the washing tower top and to recycle, the heat of purification section is all shifted out outside the system by water coolant by the diluted acid plate-type heat exchanger.The washing diluted acid of venturi scrubber with internal injection outlet, carry out solid-liquid separation through the CNII type filter, the supernatant liquor overflow is to Venturi meter diluted acid circulation groove, being pumped to Venturi meter with diluted acid then recycles, for improving solid-liquid separation effect, should add the PAM flocculation agent as the case may be, mud is discharged from the bottom, and the diluted acid of by-product takes off through desorption tower and inhales SO
2Neutralizing treatment qualified discharge is then carried out with milk of lime in the back.
The measure that the dense raising of its calcining molybdenum ore concentrate flue gas acid preparing gas is taked: 1, kiln hood adds tightness system, neither allows flue gas excessive, guarantees again not advance freezing air under little negative pressure state.2, regulate direct combustion stove gas pushing quantity and induced draft fan air balance.3, control induced draft fan air quantity is able to satisfy the normal reaction air capacity.4, controlled the dust quantity of tornado dust collector dust discharge, stopped tornado dust collector and leak out.5, scatterer dedusting mouth adds mechanically-sealing apparatus, prevents gas leakage.6. the temperature of reaction of strict control rotary kiln.
Claims (1)
1, a kind of process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln is characterized in that: adopt low-concentration sulfur dioxide to utilize unstable state relieving haperacidity technology, with the sulfur dioxide concentration that has only in the return bend kiln calcining molybdenum concentrate flue gas between the 0.1-1.5%; Guaranteeing that under the product quality premise, the concentration that improves the concentrated molybdenum ore sulfur dioxide in flue gas reaches between the 1-3%, satisfies the thermal equilibrium and the water balance that utilize unstable state relieving haperacidity;
The step that the dense raising of its calcining molybdenum ore concentrate flue gas acid preparing gas is taked:
1, kiln hood adds tightness system, neither allows flue gas excessive, guarantees again not advance freezing air under little negative pressure state;
2, regulate direct combustion stove gas pushing quantity and induced draft fan air balance;
3, control induced draft fan air quantity is able to satisfy the normal reaction air capacity;
4, control the dust quantity of tornado dust collector dust discharge well, stop tornado dust collector and leak out;
5, scatterer dedusting mouth adds mechanically-sealing apparatus, prevents gas leakage;
6. the temperature of reaction of strict control rotary kiln.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100544119A CN101306804B (en) | 2007-05-16 | 2007-05-16 | Process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100544119A CN101306804B (en) | 2007-05-16 | 2007-05-16 | Process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101306804A true CN101306804A (en) | 2008-11-19 |
| CN101306804B CN101306804B (en) | 2010-10-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007100544119A Active CN101306804B (en) | 2007-05-16 | 2007-05-16 | Process for preparing acid from flue gas by calcining molybdenum concentrate in rotary kiln |
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| CN (1) | CN101306804B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717098B (en) * | 2009-11-16 | 2011-08-17 | 阎君 | Method for preparing sodium sulfite by sulfur dioxide in tail gas generated by calcining molybdenum concentrate |
| CN105238939A (en) * | 2015-11-10 | 2016-01-13 | 李鹏飞 | Pyrogenic process arsenic removing method and device |
| CN107754596A (en) * | 2016-08-19 | 2018-03-06 | 张丽媛 | Roaster calcining discharge system gathers dust the recycling technique of sulfur dioxide in gas |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1176230C (en) * | 2002-06-28 | 2004-11-17 | 锦州市沈宏实业股份有限公司 | Process for calcining molybdenum ore concentrate |
-
2007
- 2007-05-16 CN CN2007100544119A patent/CN101306804B/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717098B (en) * | 2009-11-16 | 2011-08-17 | 阎君 | Method for preparing sodium sulfite by sulfur dioxide in tail gas generated by calcining molybdenum concentrate |
| CN105238939A (en) * | 2015-11-10 | 2016-01-13 | 李鹏飞 | Pyrogenic process arsenic removing method and device |
| CN107754596A (en) * | 2016-08-19 | 2018-03-06 | 张丽媛 | Roaster calcining discharge system gathers dust the recycling technique of sulfur dioxide in gas |
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| Publication number | Publication date |
|---|---|
| CN101306804B (en) | 2010-10-13 |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Gong Yuchuan Inventor after: Wang Honglei Inventor after: Cheng Xin Ji Inventor after: Zhang Bin Inventor after: Zhou Songquan Inventor after: Zhang Jianmin Inventor after: Zhao Xinshe Inventor before: Gong Yuchuan Inventor before: Wang Honglei Inventor before: Cheng Xin Ji |
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| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: GONG YUCHUAN WANG HONGLEI JU CHENGXIN TO: GONG YUCHUAN WANG HONGLEI JU CHENGXIN ZHANG BIN ZHOU SONGQUAN ZHANG JIANMIN ZHAO XINSHE |
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| TR01 | Transfer of patent right |
Effective date of registration: 20240117 Address after: North of Yihe, Huameishan Road, Chengdong New District, Luanchuan County, Luoyang City, Henan Province, 471000 Patentee after: China Molybdenum Co.,Ltd. Address before: River village of Luanchuan County in Henan province 471521 Miao Zi Xiang Patentee before: LUOYANG LUANCHUAN MOLYBDENUM GROUP SMELTING Co.,Ltd. |