CN101503183A - Preparation of sulphuric acid - Google Patents
Preparation of sulphuric acid Download PDFInfo
- Publication number
- CN101503183A CN101503183A CNA2009100299065A CN200910029906A CN101503183A CN 101503183 A CN101503183 A CN 101503183A CN A2009100299065 A CNA2009100299065 A CN A2009100299065A CN 200910029906 A CN200910029906 A CN 200910029906A CN 101503183 A CN101503183 A CN 101503183A
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- oxygen
- gas
- sulfuric acid
- preparation
- making
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Abstract
The invention provides a method for preparing sulphuric acid, which can effectively accelerate reaction velocity and efficiency, improve heat recovery rate, increase productivity of equipment and reduce the volume of the equipment. The method for preparing sulphuric acid comprises the steps: (1) raw ore is mixed with raw gas containing oxygen for fluidized-bed combustion to obtain intermediate gas of sulfur dioxide and oxygen; (2) the intermediate gas is dried; (3) the sulfur dioxide is transformed; in the step (1), the oxygen concentration of the raw gas is 25-50% (volume). The raw gas is formed by mixing air and oxygen. As the improvement of the invention, the oxygen is supplemented before the step (2), so that the oxygen concentration of the intermediate gas is 10-25%. The invention is the improvement of acid making technique in the process of sulfuric acid production, and has the characteristics that the method can improve the productivity of sulphuric acid making equipment with the same scale, reduce power consumption in the production and can utilize the heat produced in the technical process to the utmost extent. The invention can be used for building new factories and reconstructing old factories.
Description
Technical field
The present invention relates to a kind of preparation method of sulfuric acid.
Background technology
Existing vitriolic production technique may further comprise the steps: mix with unstripped gas in (1) raw material ore deposit, Boiling Combustion, and dry and (3) Sulphur Dioxide of (2) intermediate gas, wherein make-up gas is all used air before the Boiling Combustion in raw material ore deposit and the drying.In this technology, because major part is a nitrogen in the air, small part is an oxygen, have only oxygen to participate in reaction in sulfur process and nitrogen is not participated in reaction, the existence of a large amount of nitrogen causes reaction efficiency low, and the sulfur dioxide concentration in the intermediate gas is little, problems such as equipment is huge, and the heat recuperation rate is low.As present pyrite-based sulfuric acid production, fluidizing furnace adopts normal air to carry out roasting, because oxygen level is relatively low in the air, going out the fluidizing furnace sulfur dioxide concentration is 10%～14%, and advancing the convertor sulfur dioxide concentration is 6%～9%; Present for another example zinc ore concentrate relieving haperacidity, going out the fluidizing furnace sulfur dioxide concentration is 9%～12%, advancing the convertor sulfur dioxide concentration is 6%～7%.Lower sulfur dioxide concentration makes production unit huge, causes problems such as working cost height.
Summary of the invention
The invention provides a kind of preparation method of sulfuric acid, can effectively improve speed of response and efficient, heat recuperation rate, increase device capbility, reduce equipment volume.
Described preparation method of sulfuric acid may further comprise the steps: mix with oxygenous unstripped gas in (1) raw material ore deposit, Boiling Combustion, obtain containing the intermediate gas of sulfurous gas and oxygen, (2) intermediate gas drying, (3) Sulphur Dioxide, in the step (1), the carrier of oxygen volume concentrations in the unstripped gas is 25%～50%.
Unstripped gas is by air and oxygen mix.Wherein oxygen is made by making oxygen by air separation machine, pressure swing adsorption oxygen making device or embrane method oxygenerator.
Described raw material ore deposit is sulfurous iron ore, zinc ore concentrate, gold ore or sulphur.
As improvement of the present invention, in step (2) supplemental oxygen before, making the carrier of oxygen volume concentrations in the intermediate gas is 10%～25%.As further improving, the volume ratio of oxygen and sulfurous gas is 0.8:1～2:1 in the control intermediate gas, is preferably 0.8:1～1.5:1, more preferably 1:1～1.2:1.Wherein oxygen is made by making oxygen by air separation machine, pressure swing adsorption oxygen making device or embrane method oxygenerator.
In the present invention, the control of oxygen concentration is very important.If oxygen concentration is low excessively, corresponding furnace gas amount will increase, and reaction efficiency reduces, and causes equipment volume huge, and plant investment improves; If oxygen concentration is too high, can cause the temperature of catalyzed conversion too high, and the phosphorus/vanadium catalyst that uses in the conversion reaction have the certain temperature restriction, temperature is too high can the infringement catalyzer.
The principle of the invention is: the main reaction in fluidizing furnace of various raw materials ore deposit has
4FeS
2+11O
2＝8SO
2+2Fe
2O
3
3FeS
2+8O
2＝6SO
2+Fe
3O
4
4Fe
7S
8+53O
2＝32SO
2+14Fe
2O
3
3Fe
7S
8+38O
2＝24SO
2+7Fe
2O
3
2ZnS+3O
2＝2ZnO+2SO
2
S+O
2＝SO
2
Reaction main in convertor has
2SO
2+O
2＝2SO
3
More than reaction is thermopositive reaction, by improving the reactant concentration of oxygen, can improve speed of reaction and efficient.
Specific embodiment of the present invention is: the oxygen that produces in the oxygen generating plant becomes unstripped gas with air mixed before the furnace bottom air-blaster, wherein oxygen concentration reaches 25%～50%, unstripped gas enters the Boiling Combustion stove then, react in oxygen and raw material ore deposit, produce sulfur dioxide gas, reaction discharges heat simultaneously, goes out fluidizing furnace sulfur dioxide concentration 15%～30%.The gas that goes out fluidizing furnace reclaims heat energy, dust removal installation dedusting, enters cleaning section through waste heat boiler, restock high-concentration oxygen before entering drying tower, make the oxygen concentration in the intermediate gas reach 10%～25%, the volume ratio that makes oxygen and sulfurous gas simultaneously is 0.8:1～2:1, goes convertor to carry out Sulphur Dioxide then.
The invention has the advantages that: a, employing high-concentration oxygen carry out Boiling Combustion, have improved speed of reaction and efficient.B, owing to improved the oxygen concentration in the reactant gases, sulfur dioxide concentration improves in the furnace gas, nitrogen ratios reduces, equal sulphuric acid output appliance arrangement volume reduces.C, because nitrogen ratios reduces, and waste heat boiler gas is taken heat out of and reduced, heat energy recovery rate improves.D, because the SO3 catalytic conversion reaction carries out under comparatively high temps, and the heat that produces in the technological process can be fully used, transform workshop section superheater and economizer can be set, can reclaim than existing procedure more heat.E, because the minimizing of volume of gas has reduced systemic resistance, and reduce power consumption.
The present invention is the improvement of sulphuric acid process acid-making process, is characterized in improving the throughput of equal scale sulfuric acid apparatus, reduces the power consumption in producing, and can maximally utilise the heat that technological process produces.The present invention can be used for the construction of new factory, also can be used for modernizing and expanding the existing factory.
Development along with oxygenerating technology, the energy consumption of system oxygen and investment are all descending, this provides condition for high-concentration oxygen in the industrial production broader applications, the heat recovery efficiency that the present invention improves by oxygenation, can offset the energy consumption on system oxygen fully, for this technology realizes that industrial applications provides assurance.
Embodiment
Embodiment 1
One cover magnetic pyrite relieving haperacidity production equipment, ortho-sulfuric acid output is 60kt/a, by adopting the present invention, sulphuric acid output is brought up to 100kt/a.
The particular content of transforming is: adopt pressure swing adsorption oxygen making device, oxygen making amount is 2000Nm
3/ h.The oxygen that produces in the oxygen generating plant becomes unstripped gas with air mixed before the furnace bottom air-blaster, wherein the carrier of oxygen volume concentrations 25～35%, unstripped gas enters fluidizing furnace then, wherein oxygen and sulfurous iron ore react, generate sulfur dioxide gas, go out in the intermediate gas of fluidizing furnace, the sulfurous gas volumetric concentration is about 18%.The intermediate gas that goes out fluidizing furnace reclaims heat energy, dust removal installation dedusting, enters cleaning section through waste heat boiler, restock unstripped gas before entering drying tower, make the carrier of oxygen volume concentrations in the intermediate gas be about 18%, the sulfurous gas volumetric concentration is about 15%, the volume ratio of oxygen and sulfurous gas is 1.2:1, removing convertor then is sulphur trioxide with Sulphur Dioxide, becomes product sulfuric acid through absorbing operation again.
In this embodiment, owing to adopt preparation method of sulfuric acid of the present invention, amount of steam withdrawn is increased to 1. tons of/ton acid by 1.0 tons of/ton original acid, the steam that produces is used for generating, corresponding generated energy is increased to the acid of 260 degree/tons by 200 original degree/ton acid, if check-off system oxygen acid per ton increasing power consumption 50 degree, 1 ton of acid of every production also has the more than needed of 10 degree electricity.The comprehensive reduction that drops into aspect plant modification can obtain tangible economic benefit.
Embodiment 2
One cover zinc ore concentrate relieving haperacidity production equipment adopts sulfurization roasting, produces zinc-oxide calcine.By adopting the present invention, sulphuric acid output is brought up to 75kt/a by original 50kt/a, and simultaneous oxidation zinc baking sand quality improves.
The particular content of transforming is: adopt omnibus control system, oxygen making amount is 1500Nm
3/ a.The oxygen that produces in the oxygen generating plant becomes unstripped gas with air mixed before the furnace bottom air-blaster, wherein the carrier of oxygen volume concentrations 26～36%, unstripped gas enters fluidizing furnace then, react in oxygen wherein and raw material ore deposit, generate sulfur dioxide gas, go out in the intermediate gas of fluidizing furnace, the sulfurous gas volumetric concentration brings up to about 15% by original about 9.5%.The gas that goes out fluidizing furnace reclaims heat energy, dust removal installation dedusting, enters cleaning section through waste heat boiler, restock high-concentration oxygen before entering drying tower, make the carrier of oxygen volume concentrations be about 13.8%, the sulfurous gas volumetric concentration is about 12%, the volume ratio of oxygen and sulfurous gas is 1.15:1, removing convertor then is sulphur trioxide with Sulphur Dioxide, becomes product sulfuric acid through absorbing operation again.
Embodiment 3
-cover pyrite-based sulfuric acid production production equipment adopts the present invention, and sulphuric acid output is 100kt/a, if need invest 5,800 ten thousand yuan with traditional technology, use the present invention instead, equipment volume reduces greatly, saved civil engineering and cost of equipment, reduced the plant area area, investment is reduced to 5,000 ten thousand yuan; Simultaneously, because heat utilization efficiency improves, 1 ton of acid of every production can voluminous steam 0.5 ton, and it is sour that voluminous steam-electric power amount increases by 90 degree/tons, the power consumption that check-off system oxygen 50 degree/tons are sour, and benefit is better than traditional technology.
Concrete technology is: adopt omnibus control system, oxygen making amount is 2500Nm
3/ a.The oxygen that produces in the oxygen generating plant becomes unstripped gas with air mixed before the furnace bottom air-blaster, wherein the carrier of oxygen volume concentrations is 40～50%, unstripped gas enters fluidizing furnace then, react in oxygen wherein and raw material ore deposit, generate sulfur dioxide gas, go out in the intermediate gas of fluidizing furnace sulfurous gas volumetric concentration 27%～33%.The gas that goes out fluidizing furnace reclaims heat energy, dust removal installation dedusting, enters cleaning section through waste heat boiler, restock high-concentration oxygen before entering drying tower, make the carrier of oxygen volume concentrations be about 25%, sulfur dioxide concentration is about 25%, the volume ratio of oxygen and sulfurous gas is 1:1, removing convertor then is sulphur trioxide with Sulphur Dioxide, transforms workshop section and establishes the heat that produces in superheater and the economizer recovery conversion process.
Claims (9)
1. preparation method of sulfuric acid, may further comprise the steps: mix with oxygenous unstripped gas in (1) raw material ore deposit, Boiling Combustion, obtain containing the intermediate gas of sulfurous gas and oxygen, (2) intermediate gas drying, (3) Sulphur Dioxide is characterized in that in the step (1), the carrier of oxygen volume concentrations in the unstripped gas is 25%～50%.
2. preparation method of sulfuric acid as claimed in claim 1 is characterized in that step (2) supplemental oxygen before, and making the carrier of oxygen volume concentrations in the intermediate gas is 10%～25%.
3. preparation method of sulfuric acid as claimed in claim 2 is characterized in that step (2) supplemental oxygen before, and making the oxygen in the intermediate gas and the volume ratio of sulfurous gas is 0.8:1～2:1.
4. preparation method of sulfuric acid as claimed in claim 3 is characterized in that step (2) supplemental oxygen before, and making the oxygen in the intermediate gas and the volume ratio of sulfurous gas is 0.8:1～1.5:1.
5. preparation method of sulfuric acid as claimed in claim 4 is characterized in that step (2) supplemental oxygen before, and making the oxygen in the intermediate gas and the volume ratio of sulfurous gas is 1:1～1.2:1.
6. preparation method of sulfuric acid as claimed in claim 3 is characterized in that the oxygen that replenishes is made by making oxygen by air separation machine, pressure swing adsorption oxygen making device or embrane method oxygenerator.
7. as each described preparation method of sulfuric acid among the claim 1-6, it is characterized in that unstripped gas is made by air and oxygen mix.
8. preparation method of sulfuric acid as claimed in claim 7 is characterized in that described oxygen is made by making oxygen by air separation machine, pressure swing adsorption oxygen making device or embrane method oxygenerator.
9. as each described preparation method of sulfuric acid among the claim 1-6, it is characterized in that described raw material ore deposit is sulfurous iron ore, zinc ore concentrate, gold ore or sulphur.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100299065A CN101503183A (en) | 2009-03-23 | 2009-03-23 | Preparation of sulphuric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100299065A CN101503183A (en) | 2009-03-23 | 2009-03-23 | Preparation of sulphuric acid |
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|---|---|
| CN101503183A true CN101503183A (en) | 2009-08-12 |
Family
ID=40975573
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|---|---|---|---|
| CNA2009100299065A Pending CN101503183A (en) | 2009-03-23 | 2009-03-23 | Preparation of sulphuric acid |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101703873B (en) * | 2009-11-05 | 2012-01-18 | 周建安 | Method for reclaiming and treating flue gas desulfurization byproducts for sintered pellets |
| CN102351156A (en) * | 2011-07-28 | 2012-02-15 | 湖南科技大学 | Sulfuric acid plant production device without discharge of tail gas and process method therefor |
| CN104291276A (en) * | 2014-09-19 | 2015-01-21 | 中山市鸿程科研技术服务有限公司 | Production technology of sulphuric acid |
| CN107150999A (en) * | 2017-02-28 | 2017-09-12 | 绍兴文理学院 | A kind of technique of oxygen deprivation method Sulphuric acid |
| CN113336253A (en) * | 2021-05-24 | 2021-09-03 | 昆明理工大学 | Method for extracting aluminum oxide from high-aluminum coal gangue by using high-concentration SO2 |
| CN114981207A (en) * | 2019-11-04 | 2022-08-30 | 美卓奥图泰芬兰有限公司 | Method and apparatus for producing sulfuric acid |
-
2009
- 2009-03-23 CN CNA2009100299065A patent/CN101503183A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101703873B (en) * | 2009-11-05 | 2012-01-18 | 周建安 | Method for reclaiming and treating flue gas desulfurization byproducts for sintered pellets |
| CN102351156A (en) * | 2011-07-28 | 2012-02-15 | 湖南科技大学 | Sulfuric acid plant production device without discharge of tail gas and process method therefor |
| CN102351156B (en) * | 2011-07-28 | 2013-03-27 | 湖南科技大学 | Sulfuric acid plant production device without discharge of tail gas and process method therefor |
| CN104291276A (en) * | 2014-09-19 | 2015-01-21 | 中山市鸿程科研技术服务有限公司 | Production technology of sulphuric acid |
| CN107150999A (en) * | 2017-02-28 | 2017-09-12 | 绍兴文理学院 | A kind of technique of oxygen deprivation method Sulphuric acid |
| CN114981207A (en) * | 2019-11-04 | 2022-08-30 | 美卓奥图泰芬兰有限公司 | Method and apparatus for producing sulfuric acid |
| CN113336253A (en) * | 2021-05-24 | 2021-09-03 | 昆明理工大学 | Method for extracting aluminum oxide from high-aluminum coal gangue by using high-concentration SO2 |
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Open date: 20090812 |