CN201553609U - Sulfuric acid purifying device - Google Patents
Sulfuric acid purifying device Download PDFInfo
- Publication number
- CN201553609U CN201553609U CN2009202628378U CN200920262837U CN201553609U CN 201553609 U CN201553609 U CN 201553609U CN 2009202628378 U CN2009202628378 U CN 2009202628378U CN 200920262837 U CN200920262837 U CN 200920262837U CN 201553609 U CN201553609 U CN 201553609U
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- China
- Prior art keywords
- sulfuric acid
- interchanger
- pipeline
- raw material
- acid
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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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a sulfuric acid purifying device with low energy consumption, which comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, an evaporator and a separator formed by a pipeline and a separating sheet fixed on the pipe wall. The device is safe and simple in structure, can remove most of impurities and partial water in sulfuric acid, can achieve more than 98% of concentrated sulfuric acid, employs sulfuric acid raw materials to perform heat exchange on sulfuric acid steam, acid product and separated diluted acid, and leads sulfuric acid to be preheated sufficiently in the transportation process and achieve or approach the boiling temperature before entering into the evaporator, thereby greatly saving energy and causing power consumption of each ton of sulfuric acid to be lowered to 300 to 330 kilowatt hour.
Description
Technical field
The utility model relates to and adopts the distillation mode vitriolic production equipment of purifying.
Background technology
Existing sulfuric acid purifying plant is heated sulfuric acid after obtain the sulfuric acid of purifying after the heat exchanger heat exchange cooling by heating fumigators.The disclosed storage battery sulfuric acid production plant of China utility model specification sheets CN2159392Y is connected by acid delivering tube interior pipe electrically heated distiller with cold and hot sour interchanger, improve thermo-efficiency.Because this device heat exchange is not thorough, energy consumption is still higher, also sulfuric acid is not separated with water, and the sulfuric acid water content that obtains does not change.
Summary of the invention
The purpose of this utility model provides a kind of sulfuric acid purifying plant of less energy-consumption.
Sulfuric acid purifying plant of the present utility model comprises the vaporizer of heating sulfuric acid raw material and utilizes the interchanger of sulfuric acid cooling liberated heat to the sulfuric acid raw material preheating, interchanger comprises first interchanger and second interchanger, first interchanger is by the raw material pipeline, concentrated acid pipeline and diluted acid pipeline constitute, second interchanger is made of raw material pipeline and concentrated acid pipeline, the separator that is used for separating the sulfuric acid low boiling point component is made of pipeline and the barrier flaps that is fixed in tube wall, this separator top is communicated with the diluted acid pipeline of first interchanger, the middle part is communicated with the steam-pipe of vaporizer, the bottom is communicated with the concentrated acid pipeline of second interchanger, and the concentrated acid pipeline of second interchanger is communicated with the concentrated acid pipeline of first interchanger.
Also be connected the 3rd interchanger between above-mentioned separator and the vaporizer, the 3rd interchanger is made of steam-pipe and raw material pipeline, and steam inlet channel is communicated with vaporizer, and outlet is communicated with separator, the raw material entrance is communicated with second interchanger, and outlet is communicated with the feed port of vaporizer.
Concentrated acid pipeline in second interchanger is preferably ball bubble shape or spirrillum.Vaporizer top is the tubular buffer body of external diameter greater than the middle part, and the middle part is mounted with heating unit, and not evaporant deposit cavity is arranged at the bottom, and is connected with the advance selling pipe.
The feed(raw material)inlet of vaporizer preferably is positioned at the heating unit position at middle part.
The utility model device safety, simple to operate, most of impurity in the sulfuric acid and portion water can be removed, can obtain the vitriol oil more than 98%, adopt the sulfuric acid raw material that sulfuric acid vapor, finished acid and the diluted acid separated are carried out heat exchange, obtain abundant preheating, enter and reached before the vaporizer or near boiling temperature at course of conveying, energy efficient greatly, sulfuric acid current consumption per ton can be reduced to 300～330 kilowatt-hours.
Description of drawings
Fig. 1 is the utility model device vertical planning drawing.
Embodiment
Fig. 1 illustrates a kind of embodiment of the present utility model, is made up of first interchanger 1, second interchanger 2, the 3rd interchanger 3, vaporizer 4 and separator 5.
First interchanger 1 is made of three fluid lines: be positioned at outer field raw material pipeline 101, be positioned at the concentrated acid pipeline 102 and the diluted acid pipeline 103 of raw material pipeline 101 inner chambers.Concentrated acid pipeline 102 and diluted acid pipeline 103 can have suitable bending as " S " shape or spirrillum to increase tube wall area, improve heat exchange effect.Raw material pipeline 101 inlets are communicated with opening for feed 6, outlet connecting pipe 8, and there is acid discharge mouth 12 bottom so that salvage stores can be got rid of when device is stopped work.Concentrated acid pipeline 102 inlet connecting pipes 9, outlet is communicated with finished acid outlet 7.Diluted acid pipeline 103 inlet connecting pipes 11, outlet is communicated with diluted acid outlet 10.Export the advance selling pipe 13 that there is outer end advance selling at 7 places at finished acid, diluted acid exports the advance selling pipe 14 that there is the outer end advance selling at 10 places, makes tubing system and the external world balance that keep-ups pressure, the minimizing explosion hazard.
The 3rd interchanger 3 is made of two fluid lines: be positioned at outer field steam-pipe 301 and the raw material pipeline 302 that is positioned at steam-pipe 301 inner chambers.Raw material pipeline 302 inlet connecting pipes 15, outlet connecting pipe 18.Steam-pipe 301 inlet connecting pipes 19, outlet connecting pipe 20.
There is external diameter on vaporizer 4 tops greater than the buffer body 21 of middle part with the formation comparatively large capacity, there is heating unit 22 at the middle part, the not deposit cavity 23 of evaporant is arranged at the bottom, and the advance selling pipe 24 that is connected with outer end advance selling is so that the inside and outside pressure equilibrium of holding device, and there is not sewage draining exit 25 evaporant deposit cavity 23 bottoms so that evaporant is not got rid of in good time.Pipeline 18 inserts heating unit 22 positions, and pipeline 19 inserts the top of buffer body 21.
The sulfuric acid raw material enters the raw material pipeline 101 of first interchanger 1 from opening for feed 6, carries out heat exchange, raw material preheating for the first time with concentrated acid in the concentrated acid pipeline 102 and the diluted acid in the diluted acid pipeline 103.Flow into the raw material pipeline 201 of second interchanger 2 then through pipeline 8, carry out heat exchange with concentrated acid in the concentrated acid pipeline 202, raw material preheating for the second time, temperature further promotes.Flow into the raw material pipeline 302 of the 3rd interchanger 3 again through pipeline 15, carry out heat exchange with steam in the steam-pipe 301, raw material is preheating for the third time, and temperature promotes once more.After raw material has passed through three times preheating, temperature near in addition reach boiling temperature.Raw material after the preheating enters vaporizer 4 heating evaporations through pipeline 18 for the third time, becomes sulfuric acid vapor.
Sulfuric acid vapor enters the steam-pipe 301 of the 3rd interchanger 3 through pipeline 19, carry out the cooling first time with the raw material heat exchange in the raw material pipeline 302, the temperature of sulfuric acid vapor can be reduced to liquefaction temperature, and there is part to liquefy, become the steam that accompanies drop, enter separator 5 through pipeline 20, liquid portion is assembled on barrier flaps 502, simultaneously because a small amount of heat radiation of separator 5, part steam also condenses into liquid on barrier flaps 502, because the temperature in the separator 5 is still near the vitriolic boiling point, moisture mainly is in steam condition, has only small part with condensation of sulfuric acid, and other low-boiling point materials also are present in the steam, therefore vitriolic concentration and purity are improved in the liquid that forms, and reach concentrated refining effect.After liquid portion in the separator 5 flows out from pipeline 16, concentrated acid pipeline 202 through second interchanger 2, with sulfuric acid raw material heat exchange in the raw material pipeline 201 and cool off, enter the concentrated acid pipeline 102 of first interchanger 1 again through pipeline 9, further cool off with the sulfuric acid raw material heat exchange in the raw material pipeline 101, become finished acid near room temperature.
Vapor portion in the separator 5 flows into the diluted acid pipeline 103 of first interchanger 1 through pipeline 11 from the top of separator 5, with the sulfuric acid raw material heat exchange cooling in the raw material pipeline 101, flowing out from diluted acid outlet 10 becomes diluted acid, can be used as raw material and concentrates once more.
In the present embodiment, the technical pure rank sulfuric acid of employing 93～98% is as raw material, and the finished acid that obtains is analytical pure or other vitriol oil of higher level, concentration 98%, current consumption 300～330 kilowatt-hour/tons.
Claims (5)
1. sulfuric acid purifying plant, comprise the vaporizer of heating sulfuric acid raw material and utilize the interchanger of sulfuric acid cooling liberated heat the sulfuric acid raw material preheating, it is characterized in that, described interchanger comprises first interchanger and second interchanger, first interchanger is by the raw material pipeline, concentrated acid pipeline and diluted acid pipeline constitute, second interchanger is made of raw material pipeline and concentrated acid pipeline, the separator that is used for separating the sulfuric acid low boiling point component is made of pipeline and the barrier flaps that is fixed in tube wall, this separator top is communicated with the diluted acid pipeline of first interchanger, the middle part is communicated with the steam-pipe of vaporizer, the bottom is communicated with the concentrated acid pipeline of second interchanger, and the concentrated acid pipeline of second interchanger is communicated with the concentrated acid pipeline of first interchanger.
2. according to the described sulfuric acid purifying plant of claim 1, it is characterized in that, also be connected the 3rd interchanger between described separator and the vaporizer, the 3rd interchanger is made of steam-pipe and raw material pipeline, steam inlet channel is communicated with vaporizer, outlet is communicated with separator, and the raw material entrance is communicated with second interchanger, and outlet is communicated with the feed port of vaporizer.
3. according to the described sulfuric acid purifying plant of claim 1, it is characterized in that the concentrated acid pipeline in described second interchanger is ball bubble shape or spirrillum.
4. according to the described sulfuric acid purifying plant of claim 1, it is characterized in that the tubular buffer body of external diameter greater than the middle part arranged at described vaporizer top, there is heating unit at the middle part, and not evaporant deposit cavity is arranged at the bottom, and is connected with the advance selling pipe.
5. according to the described sulfuric acid purifying plant of claim 4, it is characterized in that the feed(raw material)inlet of described vaporizer is positioned at the heating unit position at middle part.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202628378U CN201553609U (en) | 2009-11-10 | 2009-11-10 | Sulfuric acid purifying device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202628378U CN201553609U (en) | 2009-11-10 | 2009-11-10 | Sulfuric acid purifying device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201553609U true CN201553609U (en) | 2010-08-18 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202628378U Expired - Lifetime CN201553609U (en) | 2009-11-10 | 2009-11-10 | Sulfuric acid purifying device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201553609U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102728082A (en) * | 2012-07-04 | 2012-10-17 | 朱大春 | Steam evaporating, concentrating and crystallizing system without live steam |
| CN102826518A (en) * | 2011-06-15 | 2012-12-19 | 安徽理工大学 | Concentrated waste acid recovery technology |
| CN104085861A (en) * | 2014-07-11 | 2014-10-08 | 昆山明宽环保节能科技有限公司 | Device for recovering sulfuric acid from graphene acid-containing wastewater and corresponding technique thereof |
| CN111591961A (en) * | 2020-06-19 | 2020-08-28 | 贵溪市恒盛实业有限公司 | Concentrated sulfuric acid purification equipment and purification process applying same |
| CN114558335A (en) * | 2022-03-17 | 2022-05-31 | 盛隆资源再生（无锡）有限公司 | Sulfuric acid concentration system device and concentration method |
-
2009
- 2009-11-10 CN CN2009202628378U patent/CN201553609U/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102826518A (en) * | 2011-06-15 | 2012-12-19 | 安徽理工大学 | Concentrated waste acid recovery technology |
| CN102826518B (en) * | 2011-06-15 | 2014-05-28 | 安徽理工大学 | Concentrated waste acid recovery technology |
| CN102728082A (en) * | 2012-07-04 | 2012-10-17 | 朱大春 | Steam evaporating, concentrating and crystallizing system without live steam |
| CN102728082B (en) * | 2012-07-04 | 2014-06-25 | 朱大春 | Steam evaporating, concentrating and crystallizing system without live steam |
| CN104085861A (en) * | 2014-07-11 | 2014-10-08 | 昆山明宽环保节能科技有限公司 | Device for recovering sulfuric acid from graphene acid-containing wastewater and corresponding technique thereof |
| CN111591961A (en) * | 2020-06-19 | 2020-08-28 | 贵溪市恒盛实业有限公司 | Concentrated sulfuric acid purification equipment and purification process applying same |
| CN114558335A (en) * | 2022-03-17 | 2022-05-31 | 盛隆资源再生（无锡）有限公司 | Sulfuric acid concentration system device and concentration method |
| CN114558335B (en) * | 2022-03-17 | 2024-03-12 | 盛隆资源再生（无锡）有限公司 | Sulfuric acid concentration system device and concentration method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 515064 Guangdong city of Shantou province Chaoshan Road West Long Street No. 1-3 Patentee after: XILONG SCIENTIFIC CO., LTD. Address before: 515064 Guangdong city of Shantou province Chaoshan Road West Long Street No. 1-3 Patentee before: Xilong Chemical Co., Ltd. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20100818 |
|
| CX01 | Expiry of patent term |