CN101475147A - Dilute sulphuric acid concentration method and system - Google Patents
Dilute sulphuric acid concentration method and system Download PDFInfo
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- CN101475147A CN101475147A CNA2009100369320A CN200910036932A CN101475147A CN 101475147 A CN101475147 A CN 101475147A CN A2009100369320 A CNA2009100369320 A CN A2009100369320A CN 200910036932 A CN200910036932 A CN 200910036932A CN 101475147 A CN101475147 A CN 101475147A
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- sulphuric acid
- dilute sulphuric
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention provides a dilute sulphuric acid condensation method and a system. Because the method of directly contacting dilute sulphuric acid and water vapor at a temperature higher than the boiling point of the dilute sulphuric acid to evaporate and condense, the heat exchange is direct and quick, the method not only saves an expensive heat exchanger, but also saves a water ring type vacuum pump and a high-temperature concentrated sulphuric acid resistant circulating pump, simplifies a condensation system greatly, and lowers equipment investment cost; in addition, part of the water vapor evaporated from the dilute sulphuric acid is used as a heat source of other manufacturing processes, and the other part of the water vapor is recycled, so that the condensation of the dilute sulphuric acid becomes a technological process with energy consumption close to zero, namely, the condensation of the dilute sulphuric acid becomes an energy-free process.
Description
Technical field
The invention belongs to chemical field, particularly, relate to a kind of concentration method and system of dilute sulphuric acid.
Background technology
Sulfuric acid is of many uses in industries such as chemical industry, iron and steel.But in the major applications process, exhausted sulfuric acid becomes and contains assorted dilute sulphuric acid.These dilute sulphuric acids will cause water body or soil acidification as just being discharged in the environment without handling, and the harm ecotope is wasted resource in a large number.Past, the normal modes such as generating gypsum or production phosphate fertilizer that adopts was handled dilute sulphuric acid, but needs along with the development and the environmental protection of chemical industry, this processing mode can't meet the demands, the substitute is dilute sulphuric acid concentrated after, recycling, present method is because of avoiding environmental pollution, and excellent specific property such as economize on resources is subjected to people and praises highly.
The spissated method of dilute sulphuric acid mainly contains two kinds, a kind of is that dilute sulphuric acid is placed vaporizer, under condition of normal pressure, directly heat with the fuel heating fumigators or with interchanger, apply for a patent in " the concentrating and impurity removing method of dilute sulphuric acid in the Titanium White Production By Sulfuric Acid Process process " (publication number is CN101214931A) as China, under the normal pressure, the steam concentration systems that adopts heating graphite tubular heat exchange to constitute reaches heating vitriolic purpose wherein; Another kind is to concentrate with interchanger heating dilute sulphuric acid under reduced pressure, as US5, and 228,885, disclosed a kind ofly under reduced pressure, carry out spissated method and apparatus with interchanger heating dilute sulphuric acid.In a word, at present concentrating of dilute sulphuric acid all is that method by indirect heating realizes.Because the pyritous sulfuric acid particularly pyritous vitriol oil has intensive corrodibility, the material of this heat exchanging device has proposed high requirement, needs expensive rare metal such as tantalum, zirconium and specific alloy to make interchanger; Decompression is carried in the dense process and is used water-ring vacuum pump, has not only caused to carry dense steam and can't recycle, and has wasted a large amount of water of condensation; In addition, indirect heating also needs the recycle pump of the high temperature resistant vitriol oil, and these have all improved the spissated cost of dilute sulphuric acid, thereby has limited the recycling of useless dilute sulphuric acid.
Summary of the invention
In order to overcome the high shortcoming of cost that causes owing to the employing indirect heating in the at present useless dilute sulphuric acid concentration process, the present invention proposes a kind of dilute sulphuric acid concentration method.
Another object of the present invention provides a kind of dilute sulphuric acid concentration systems.
For achieving the above object, dilute sulphuric acid concentration method provided by the invention may further comprise the steps:
(1) dilute sulphuric acid is injected vaporizer;
(2) in described vaporizer, feed the water vapor that temperature is higher than the dilute sulphuric acid boiling point, water vapor and dilute sulphuric acid are directly contacted carry out heat exchange,, thereby dilute sulphuric acid is concentrated the evaporation of the water in the dilute sulphuric acid.
Described vaporizer comprises 1st effective evaporator, 2nd effect evaporator and the triple-effect evaporator that interconnects, described water vapor at first feeds 1st effective evaporator, the steam that ejects from 1st effective evaporator feeds 2nd effect evaporator again, and the steam that ejects from 2nd effect evaporator feeds triple-effect evaporator again.
From the steam separated into two parts that described triple-effect evaporator ejects, a part of steam uses for other technologies as thermal source, and another part steam is heated to temperature once more and is higher than the dilute sulphuric acid boiling point and feeds 1st effective evaporator and carry out recycle.
Described dilute sulphuric acid evaporation concentration is to carry out under condition of normal pressure.
Described water vapor is that temperature is roughly 400～700 ℃ near non-pressurized superheated vapour.
Dilute sulphuric acid concentration systems provided by the invention comprises:
Boiler, described boiler is heated into the water vapor that temperature is higher than the dilute sulphuric acid boiling point with water;
Vaporizer holds dilute sulphuric acid in the described vaporizer;
Intake line, described intake line are communicated with described boiler and described vaporizer, and the water vapor that comes out from described boiler feeds vaporizer by intake line, directly contact with dilute sulphuric acid; And
First delivery conduit, described first delivery conduit is communicated with described vaporizer and described boiler, and the steam that ejects from described vaporizer enters the boiler recycle once more by first delivery conduit.
Preferably, described vaporizer comprises 1st effective evaporator, 2nd effect evaporator and the triple-effect evaporator that interconnects, and described intake line connects described boiler and described 1st effective evaporator, and described first delivery conduit connects described triple-effect evaporator and described boiler.
Described triple-effect evaporator also is provided with second delivery conduit, connects the equipment that needs thermal source, from
The steam that described triple-effect evaporator ejects by second delivery conduit to the equipment heat supply that needs thermal source.
The present invention carries out evaporation concentration because the water vapor that adopts dilute sulphuric acid and temperature to be higher than the dilute sulphuric acid boiling point directly contacts, thermal exchange directly, rapidly, not only saved expensive heat exchanger, and saved the recycle pump of the water-ring vacuum pump and the high temperature resistant vitriol oil, simplify concentration systems greatly, reduced equipment investment cost; A water vapor part that is evaporated from dilute sulphuric acid in addition reclaims the thermal source as other technological process, another part returns vaporizer and carries out recycle, carrying of dilute sulphuric acid is dense to become the technological process that an energy consumption is close to zero thereby make, that is to say that the present invention makes that carrying of dilute sulphuric acid is dense to become a process that the energy is free substantially.
Description of drawings
Fig. 1 is the structural representation of sulphuric acid concentration first embodiment of system of the present invention;
Fig. 2 is the structural representation of sulphuric acid concentration second embodiment of system of the present invention.
Embodiment
Ultimate principle of the present invention is: in vaporizer, dilute sulphuric acid directly contacts with the water vapor that temperature is higher than the dilute sulphuric acid boiling point, high-temperature water vapor directly sends heat in the dilute sulphuric acid water, make it to become water vapour, and common water vapor evaporation with lesser temps, separate with sulfuric acid, thereby reach the spissated purpose of dilute sulphuric acid; The final lower water vapor separated into two parts of temperature of from vaporizer, discharging, a part is used for other technologies as thermal source, and another part returns the boiler recycle, further concentrates dilute sulphuric acid.
As shown in Figure 1, be first embodiment of dilute sulphuric acid concentration systems of the present invention, this dilute sulphuric acid concentration systems comprises: boiler 1 is heated into water the water vapor that temperature is higher than the dilute sulphuric acid boiling point in described boiler; Vaporizer 2 holds dilute sulphuric acid in the described vaporizer; Intake line 3, described intake line are communicated with described boiler and described vaporizer, and the water vapor that comes out from described boiler feeds vaporizer by intake line, directly contact with dilute sulphuric acid; And first delivery conduit 41, described first delivery conduit is communicated with described vaporizer and described boiler, and the steam that ejects from described vaporizer enters the boiler recycle once more by first delivery conduit.
Fig. 2 is second embodiment of dilute sulphuric acid concentration systems of the present invention, different with first embodiment is, described vaporizer comprises 1st effective evaporator 21,2nd effect evaporator 22 and the triple-effect evaporator 23 that interconnects, described intake line 3 connects described boiler and described 1st effective evaporator, and described first delivery conduit 41 connects described triple-effect evaporator 23 and described boiler 1.
Described triple-effect evaporator also is provided with second delivery conduit 42, connects the equipment 5 need thermal source, the steam that ejects from described triple-effect evaporator by second delivery conduit 42 to the equipment heat supply 5 that needs thermal source.
To the spissated method of dilute sulphuric acid, difference is as follows with described dilute sulphuric acid concentration systems for detailed description below:
With reference to Fig. 1, in described boiler 1, add entry; 25% dilute sulphuric acid is packed in the ceramic evaporator 2; Water in the heating boiler is 400 ℃ of superheated vapours near normal pressure (gauge pressure 10KPa); Superheated vapour directly feeds in the dilute sulphuric acid in the described ceramic evaporator 2 by described intake line 3, heat is passed to water in the dilute sulphuric acid, water in the dilute sulphuric acid is evaporated under condition of normal pressure, the water at low temperature steam returns boiler by first delivery conduit 41 and carries out recycle, or, for needing the equipment 5 of thermal source, other provide thermal source or discharge, after after a while through second delivery conduit 42, moisture in the dilute sulphuric acid partly is evaporated, and obtains 50% sulfuric acid.
With reference to Fig. 2, in described boiler 1, add entry; 25% the dilute sulphuric acid described 1st effective evaporator 21 of packing into, 2nd effect evaporator 22 is in the triple-effect evaporator 23; Water in the heating boiler is 700 ℃ of superheated vapours near normal pressure (gauge pressure 10KPa); Superheated vapour directly feeds in the dilute sulphuric acid in the described 1st effective evaporator 21 by described intake line 3, and heat is passed to water in the dilute sulphuric acid, and the interior water of dilute sulphuric acid is evaporated under condition of normal pressure; From the water at low temperature steam of 1st effective evaporator 21 output directly feeds dilute sulphuric acid the described 2nd effect evaporator 22 by described intake line 3 in, heat is passed to water in the dilute sulphuric acid, the interior water of dilute sulphuric acid is evaporated under condition of normal pressure; From the water at low temperature steam of 2nd effect evaporator 22 output directly feeds dilute sulphuric acid the described triple-effect evaporator 23 by described intake line 3 in, heat is passed to water in the dilute sulphuric acid, the interior water of dilute sulphuric acid is evaporated under condition of normal pressure; Return boiler from the water at low temperature steam of triple-effect evaporator 23 output by first delivery conduit 41 and carry out recycle, or through second delivery conduit 42, for needing the equipment 5 of thermal source, other provide thermal source or discharge, after after a while, moisture in the dilute sulphuric acid partly is evaporated, and obtains concentration and be 75% sulfuric acid in 1st effective evaporator.
To sum up, dilute sulphuric acid concentration method of the present invention may further comprise the steps:
(1) dilute sulphuric acid is injected vaporizer;
(2) in described vaporizer, feed the water vapor that temperature is higher than the dilute sulphuric acid boiling point, water vapor and dilute sulphuric acid are directly contacted carry out heat exchange,, thereby dilute sulphuric acid is concentrated the evaporation of the water in the dilute sulphuric acid.
High-temperature water vapor directly sends heat in the dilute sulphuric acid water, makes it to become water vapour, and jointly with the water vapor evaporation of lesser temps, separates with sulfuric acid, thereby reach the spissated purpose of dilute sulphuric acid.
From the steam separated into two parts that described triple-effect evaporator ejects, a part of steam uses for other technologies as thermal source, and another part steam is heated to temperature once more and is higher than the dilute sulphuric acid boiling point and feeds 1st effective evaporator and carry out recycle.
Because final water vapor of discharging still contains a spot of sulfuric acid vapor, in order equipment not to be caused corrosion, this two-way steam need pass through unslaked lime or white lime, and wherein sulfuric acid vapor is sponged.Particularly, the water vapor that is evaporated from dilute sulphuric acid reclaims the thermal source as other technological process, or Returning evaporimeter recycle, carrying of dilute sulphuric acid is dense to become the technology that an energy consumption is close to zero thereby make, that is to say that the present invention makes that carrying of dilute sulphuric acid is dense to become a process that the energy is free substantially.
Owing to adopt multi-effect evaporation system, can reduce the consumption of high-temperature water vapor, and can reduce the content of sulfuric acid vapor in the water vapor that finally from vaporizer, ejects.
Described vaporizer carries out the evaporation of moisture under condition of normal pressure.Evaporator themself should adopt the material preparation that possesses high temperature resistant vitriol oil corrosive nature, and as pottery, graphite etc. to having relatively high expectations of vaporizer matter material, as increasing withstand voltage properties again, will increase the equipment investment cost of vaporizer.
Described temperature is higher than the water vapor of dilute sulphuric acid boiling point preferably near non-pressurized superheated vapour.Vaporizer is to work under condition of normal pressure, as long as superheated vapour can overcome on-way resistance, promptly the pressure ratio normal pressure is high slightly in other words near normal pressure.
The foregoing description is preferred embodiment of the present invention, is not to be used for limiting the scope of the present invention, so all equivalences of being done with the described structure of claim of the present invention, feature and principle change or modify, all should be included within the claim scope of the present invention.
Claims (8)
1. a dilute sulphuric acid concentration method is characterized in that, may further comprise the steps:
(1) dilute sulphuric acid is injected vaporizer;
(2) in described vaporizer, feed the water vapor that temperature is higher than the dilute sulphuric acid boiling point, water vapor and dilute sulphuric acid are directly contacted carry out heat exchange,, thereby dilute sulphuric acid is concentrated the evaporation of the water in the dilute sulphuric acid.
2. dilute sulphuric acid concentration method as claimed in claim 1, it is characterized in that, described vaporizer comprises 1st effective evaporator, 2nd effect evaporator and the triple-effect evaporator that interconnects, described water vapor at first feeds 1st effective evaporator, the steam that ejects from 1st effective evaporator feeds 2nd effect evaporator again, and the steam that ejects from 2nd effect evaporator feeds triple-effect evaporator again.
3. dilute sulphuric acid concentration method as claimed in claim 2, it is characterized in that, the steam separated into two parts that ejects from described triple-effect evaporator, for the use of other technologies, another part steam is heated to temperature and is higher than the dilute sulphuric acid boiling point and feeds 1st effective evaporator and carry out recycle part steam once more as thermal source.
4. dilute sulphuric acid concentration method as claimed in claim 1 is characterized in that, described dilute sulphuric acid evaporation concentration is to carry out under condition of normal pressure.
5. dilute sulphuric acid concentration method as claimed in claim 1 is characterized in that, described water vapor is that temperature is roughly 400～700 ℃ near non-pressurized superheated vapour.
6. a dilute sulphuric acid concentration systems is characterized in that, comprising:
Boiler, described boiler is heated into the water vapor that temperature is higher than the dilute sulphuric acid boiling point with water;
Vaporizer holds dilute sulphuric acid in the described vaporizer;
Intake line, described intake line are communicated with described boiler and described vaporizer, and the water vapor that comes out from described boiler feeds vaporizer by intake line, directly contact with dilute sulphuric acid; And
First delivery conduit, described first delivery conduit is communicated with described vaporizer and described boiler, and the steam that ejects from described vaporizer enters the boiler recycle once more by first delivery conduit.
7. dilute sulphuric acid concentration systems as claimed in claim 6, it is characterized in that, described vaporizer comprises 1st effective evaporator, 2nd effect evaporator and the triple-effect evaporator that interconnects, described intake line connects described boiler and described 1st effective evaporator, and described first delivery conduit connects described triple-effect evaporator and described boiler.
8. dilute sulphuric acid concentration systems as claimed in claim 9, it is characterized in that, described triple-effect evaporator also is provided with second delivery conduit, connects the equipment need thermal source, the steam that ejects from described triple-effect evaporator by second delivery conduit to the equipment heat supply that needs thermal source.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100369320A CN101475147A (en) | 2009-01-23 | 2009-01-23 | Dilute sulphuric acid concentration method and system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100369320A CN101475147A (en) | 2009-01-23 | 2009-01-23 | Dilute sulphuric acid concentration method and system |
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| CN101475147A true CN101475147A (en) | 2009-07-08 |
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| CNA2009100369320A Pending CN101475147A (en) | 2009-01-23 | 2009-01-23 | Dilute sulphuric acid concentration method and system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101935077A (en) * | 2010-08-27 | 2011-01-05 | 南通京通石墨设备有限公司 | Waste acid concentration multistage treatment method |
| CN114653080A (en) * | 2022-05-07 | 2022-06-24 | 南通星球石墨股份有限公司 | Carborundum sulphuric acid concentration evaporator |
-
2009
- 2009-01-23 CN CNA2009100369320A patent/CN101475147A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101935077A (en) * | 2010-08-27 | 2011-01-05 | 南通京通石墨设备有限公司 | Waste acid concentration multistage treatment method |
| CN114653080A (en) * | 2022-05-07 | 2022-06-24 | 南通星球石墨股份有限公司 | Carborundum sulphuric acid concentration evaporator |
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Open date: 20090708 |