CN104876194A - Method for recycling sulfuric acid and sulfate by sulfate-containing dilute sulfuric acid - Google Patents
Method for recycling sulfuric acid and sulfate by sulfate-containing dilute sulfuric acid Download PDFInfo
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- CN104876194A CN104876194A CN201510294930.7A CN201510294930A CN104876194A CN 104876194 A CN104876194 A CN 104876194A CN 201510294930 A CN201510294930 A CN 201510294930A CN 104876194 A CN104876194 A CN 104876194A
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- sulfate
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Abstract
The invention discloses a method for recycling sulfuric acid and sulfate by sulfate-contained dilute sulfuric acid. The method includes the steps that the sulfate-contained dilute sulfuric acid is subjected to vacuum concentration, precipitant is added in the sulfate-contained dilute sulfuric acid subjected to vacuum concentration, the sulfate is crystalized out, solid-liquid separation is performed to obtain the sulfate and dilute sulfuric acid filtrate, part of the precipitant recycled from the obtained dilute sulfuric acid filtrate via distilling is reused in the crystalizing process, and the left dilute sulfuric acid after distilling is subjected to concentration treatment to obtain a needed concentrated sulfuric acid product. The method for recycling the sulfuric acid and the sulfate by the sulfate-contained dilute sulfuric acid has the advantages that the sulfuric acid in the sulfate-contained dilute sulfuric acid can be recycled, the sulfate ingredient in the dilute sulfuric acid can be recycled, raw materials for production are easy to obtain, and the method is technically simple to control.
Description
Technical field
The present invention relates to a kind for the treatment of process of containing sulfate dilute sulphuric acid, particularly a kind ofly utilize the reclaim(ed) sulfuric acid salt of containing sulfate dilute sulphuric acid and the novel process for comprehensively treating of sulfuric acid.
Background technology
The recycling of current containing sulfate dilute sulphuric acid is a technical barrier always.Such as common just have containing salt Waste Sulfuric Acid: the (1) salty scrap acid that produces of titanium dioxide Production By Sulfuric Acid Process, containing a large amount of vitriol such as ferrous sulfate, magnesium sulfate in this spent acid; (2), in diazotization reaction, using sulfuric acid as souring agent, produce nitrous acid and carry out, in diazotizing technological process, producing the Waste Sulfuric Acid of a large amount of contains sodium sulfate or potassium sulfate.This type of containing sulfate spent acid saltiness is all close to saturation concentration, and usual way is difficult to process, and recognize according to the patent of having consulted and periodical literature, the process containing salt spent acid mainly contains following several means: 1, condensing crystal method.In " Huzhou Vocational Technology College's journal ", Wang Qing utilizes the dissolubility data of ferrous sulfate in sulphuric acid soln, secondary concentration method is adopted to carry out the removal of vitriol and the recovery of sulfuric acid to titanium white waste acid, experiment shows that spent acid is after separation ferrous sulfate, its sulfuric acid content can reach 80%(w), can be used in Producing Titanium Dioxide; In Chinese patent 201010561886, University Of Chongqing utilizes sedimentation pre-treatment, one section of flash distillation-crystallization concentrating and separating, two sections of vacuum evaporations are separated and are separated with three sections of vacuum evaporations, reclaim(ed) sulfuric acid and sulfate product.Such condensing crystal process titanium white waste acid method, energy consumption is higher, and all needing provides high temperature to carry out concentrated vitriol content, separates out vitriol; And in condensing crystal process, easily causing concentrated wall fouling, line clogging, solidliquid mixture is difficult to the problems such as conveying.2, evaporative freezing crystallization process.In " Treatment of Industrial Water ", Chen Wensong, Ning Xunan, Bai Xiaoyan mention and adopt freeze crystallization process sulfuric acid pickling waste liquid.This method utilizes vitriol in sulphuric acid soln, along with the reduction of temperature, the physical property that vitriol solubleness also decreases, after moisture in evaporation dilute sulphuric acid, improve sulfuric acid content, after giving evaporation, material is with frozen cooling process simultaneously, reduces the solubleness of vitriol in sulfuric acid, separate out sulphate finished product, and reclaim the sulfuric acid obtaining the low impurity of high-content.Though the operation of this method strong adaptability, technically reliable, spent acid process energy consumption is high, and cold insulation requires high, and equipment is many, is difficult to promote on a large scale.3, extraction process.In Chinese patent 94190556, Nittetsu Mining Co., Ltd. utilizes solvent extraction to dispose titanium in Titanium White Production By Sulfuric Acid Process spent acid, then carries out diffusion dialysis process to the solution after extraction.This method technological operation is simple, but can only extract the titanium component in spent acid, and cannot be separated other sulfate impurities, the scope of application is little.4, one-step calcinations.There is the high temperature energy mentioned and utilize coal-fired or fuel gas buring in Chinese patent 201110093594, take temperature control gasification absorption technique reclaim(ed) sulfuric acid.Whole technique is made up of operation of burning, gasification cleaning section, absorption operation, waste heat recovery operation and vent gas treatment operation.This method gained sulfuric acid is purer, and reclaim(ed) sulfuric acid is controlled, and the vitriol in spent acid is separated with solid phase.But this method vent gas treatment is not good at easily causing secondary pollution, complicated operation, equipment erosion resistance requires high.
Summary of the invention
Object of the present invention is exactly for above-mentioned the deficiencies in the prior art, provides a kind of method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol that treatment process controls simply, starting material are easy to get.
The technical solution used in the present invention is as follows:
A kind of method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol, it is characterized in that its method steps the following is: first by containing sulfate dilute sulphuric acid vacuum concentration, then precipitation agent is added in the containing sulfate dilute sulphuric acid after above-mentioned vacuum concentration, crystallization vitriol, carry out solid-liquid separation afterwards, obtain vitriol and dilute sulphuric acid filtrate, the partly precipitated agent that the dilute sulphuric acid filtrate of gained is obtained by Distillation recovery is back to above-mentioned crystallisation process, and dilute sulphuric acid remaining after distillation is by obtaining required vitriol oil product after concentration.
Vitriol in described containing sulfate dilute sulphuric acid is sodium sulfate, potassium sulfate or ferrous sulfate, and the sulfuric acid massfraction in this containing sulfate dilute sulphuric acid is 20-60%.
Described precipitation agent is methyl alcohol, ethanol, acetone, acetic acid or ethylene glycol.
Vitriol in the rare sulphur sulphur of described containing sulfate is sodium sulfate or potassium sulfate, and the precipitation agent of employing is methyl alcohol, ethanol or acetone, and the volume ratio of described dilute sulphuric acid and precipitation agent is 1:1-1:3.
Vitriol in the rare sulphur sulphur of described containing sulfate is ferrous sulfate, and the precipitation agent of employing is acetone, and the volume ratio of described dilute sulphuric acid and precipitation agent is 1:1-1:2.5.
The vitriol obtained after described solid-liquid separation adopts described precipitation agent to be that washing composition repeatedly washs, until washing after filtrate in sulfuric acid massfraction content lower than 0.5%, again carry out solid-liquid separation afterwards, obtain required sulfate product.
Described dilute sulphuric acid filtrate adopts air distillation to reclaim and obtains partly precipitated agent, and dilute sulphuric acid remaining after distillation adopts underpressure distillation vacuum concentration to obtain the vitriol oil.
The invention has the beneficial effects as follows:
The present invention had both reclaimed the sulfuric acid in containing sulfate dilute sulphuric acid, had reclaimed again the vitriol composition in dilute sulphuric acid.The starting material produced are easy to get, and technology controlling and process is simple.Compared with prior art, the present invention not only solves the emission problem of containing sulfate dilute sulphuric acid, can turn waste into wealth again.Prior art is except directly neutralizing containing sulfate dilute sulphuric acid except discharge, and be mostly adopt concentration salty scrap acid, energy consumption is high, and desalination rate is low.Comparatively advanced is exactly adopt extraction process, the vitriol in extraction and recovery salty scrap acid, but the specific aim of extraction agent is comparatively strong, can not be popularized on a large scale.The present invention is compared with the related process of existing containing sulfate dilute sulphuric acid process, and the process for containing sulfate dilute sulphuric acid provides a new way, and when processing containing sulfate dilute sulphuric acid, many methods are available.
Accompanying drawing explanation
Fig. 1 is the technological process block-diagram of containing sulfate dilute sulphuric acid precipitator method treatment process of the present invention.
In Fig. 1,1, concentration kettle; 2, stillpot; 3, strainer; 4, filtrate surge tank; 5, distillation tower; 6, concentration kettle; 7, vacuum pump; 8, moisture eliminator.
Embodiment
Below in conjunction with specific embodiments and the drawings, the invention will be further described:
In following examples, the clearance of vitriol is balanced by the total mass of sulfate ion, determines about the acid base titration of sulfuric acid, the gravimetric analysis of sulfate ion.
The metric calculation shown in following table is as follows:
Sulphate content (%)=total sulfate radical content-sulfuric acid content;
Sulphate content × ortho-sulfuric acid weight in ortho-sulfate amount=ortho-sulfuric acid;
The rear sulfuric acid weight of sulphate content × process in the rear sulfuric acid of vitriol amount=process after process;
Clearance (%)=100 × (after ortho-sulfate amount-process vitriol amount)/ortho-sulfate amount of vitriol.
Concrete method steps is: first by containing sulfate dilute sulphuric acid vacuum concentration in concentration kettle 1, makes sulfuric acid massfraction be 20-60%.Then the containing sulfate dilute sulphuric acid after above-mentioned vacuum concentration is transported in crystallization kettle 2, adds precipitation agent wherein, crystallization vitriol, and vitriol is sodium sulfate, potassium sulfate or ferrous sulfate, and precipitation agent is then methyl alcohol, ethanol, acetone, acetic acid or ethylene glycol.Vitriol be sodium sulfate or potassium sulfate time, the precipitation agent of employing is methyl alcohol, ethanol or acetone, and the volume ratio of dilute sulphuric acid and precipitation agent is 1:1-1:3.Vitriol is ferrous sulfate, and the precipitation agent of employing is acetone, and the volume ratio of dilute sulphuric acid and precipitation agent is 1:1-1:2.5.Solid-liquid separation is carried out with strainer 3 after sulphate crystal is separated out, obtain vitriol and dilute sulphuric acid filtrate, the vitriol obtained after solid-liquid separation can adopt used precipitation agent repeatedly to wash for washing composition, until in filtrate after washing sulfuric acid massfraction content lower than 0.5%.Required sulfate product is packaged to be after vitriol moisture eliminator 8 drying after washing.Dilute sulphuric acid filtrate enters distillation tower 5 after entering filtrate surge tank 4 again, adopt air distillation reclaim obtain partly precipitated agent be back to above-mentioned crystallisation process or for washing, dilute sulphuric acid remaining after distillation enters concentration kettle 6, is acted on adopt underpressure distillation vacuum concentration to obtain vitriol oil product by vacuum pump 7.
Embodiment 1: separate out the sodium sulfate in dilute sulphuric acid with ethanol:
Under lower routine method condition, use ethanol to be removed by sodium sulfate in dilute sulphuric acid as precipitation agent: in dilute sulphuric acid, sulfuric acid content is 23.18 %, and sodium sulphate content is 9.73%, this dilute sulphuric acid concentrated is to different concns, and the ratio between sulfuric acid and sulphate content is constant.Adding dilute sulphuric acid with ethanol contend ratio is the ethanol of 1: 2, under normal temperature and pressure conditions, stirs maintenance 1 hour, Precipitation solid sodium sulfate.Under different sulfuric acid concentration, the clearance of sodium sulfate is displayed in Table 1:
Table 1:
| Sulfuric acid content | Sodium sulphate content | Sodium sulfate clearance |
| 23.18 % | 9.83% | 46.19% |
| 34.29% | 14.54% | 75.14% |
| 44.15% | 18.72% | 82.81% |
| 50.21% | 21.29% | 90.02% |
These results prove, the paramount desalination rate of sodium sulfate in vitriol removed by ethanol, to need to improve in dilute sulphuric acid more than sulfuric acid content to 35%.
On the basis of above experiment, selected sulfuric acid content is 47.08 %, and sodium sulphate content is 20.37%, adds different dilute sulphuric acids and ethanol contend than ethanol, separates out solid sodium sulfate.Different volumes ratio, the clearance of sodium sulfate shows in table 2.
Table 2:
| Sulfuric acid content | Sodium sulphate content | Acid alcohol volume ratio | Desalination rate |
| 47.08 % | 20.37 % | 1:1 | 82.27 % |
| 47.08 % | 20.37 % | 1:1.5 | 89.08% |
| 47.08 % | 20.37 % | 1:2 | 89.32% |
| 47.08 % | 20.37 % | 1:2.5 | 90.39% |
| 47.08 % | 20.37 % | 1:3 | 90.50% |
These results prove, sodium sulfate in sulfuric acid removed by ethanol, and acid alcohol volume ratio should in 1.5-2.5 scope class.To sum up, sodium sulfate in sulfuric acid removed by ethanol, and sulfuric acid content need more than 35%, and sulfuric acid and ethanol contend are than between 1.5-2.5.
Example 2: separate out the ferrous sulfate in dilute sulphuric acid with acetone:
Under lower routine method condition, acetone is used to be removed by ferrous sulfate in sulfuric acid as precipitation agent: sulfuric acid content 22.91 % in dilute sulphuric acid, ferrous sulfate 8.28 %, adopt different sulfuric acid-acetone volume ratio to do Precipitation ferrous sulfate, show that related data is in table 3.
Table 3:
| Sulfuric acid-acetone volume ratio | Ferrous sulfate clearance |
| 1:1.5 | 67.01% |
| 1:2 | 74.45% |
| 1:2.5 | 76.52% |
These results prove: in dilute sulphuric acid, and use acetone to remove ferrous sulfate, sulfuric acid-acetone volume ratio should control between 2-2.5.
Comprehensive above two groups of examples, in dilute sulphuric acid, different types of vitriol can select different solvents as precipitation agent, removes the vitriol in sulfuric acid; And the clearance of volume ratio between different dilute sulphuric acid and solvent and vitriol also has certain dependency.
Other the undeclared part that the present invention relates to adopts prior art to be realized.
Claims (7)
1. one kind utilizes the method for containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol, it is characterized in that its method steps the following is: first by containing sulfate dilute sulphuric acid vacuum concentration, then precipitation agent is added in the containing sulfate dilute sulphuric acid after above-mentioned vacuum concentration, crystallization vitriol, carry out solid-liquid separation afterwards, obtain vitriol and dilute sulphuric acid filtrate, the partly precipitated agent that the dilute sulphuric acid filtrate of gained is obtained by Distillation recovery is back to above-mentioned crystallisation process, and dilute sulphuric acid remaining after distillation is by obtaining required vitriol oil product after concentration.
2. the method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol according to claim 1, it is characterized in that the vitriol in described containing sulfate dilute sulphuric acid is sodium sulfate, potassium sulfate, ferrous sulfate, the sulfuric acid massfraction in this containing sulfate dilute sulphuric acid is 20-60%.
3. the method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol according to claim 1 and 2, is characterized in that described precipitation agent is methyl alcohol, ethanol, acetone, acetic acid or ethylene glycol.
4. the method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol according to claim 2, it is characterized in that the vitriol in the rare sulphur sulphur of described containing sulfate is sodium sulfate or potassium sulfate, the precipitation agent adopted is methyl alcohol, ethanol or acetone, and the volume ratio of described dilute sulphuric acid and precipitation agent is 1:1-1:3.
5. the method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol according to claim 2, it is characterized in that the vitriol in the rare sulphur sulphur of described containing sulfate is ferrous sulfate, the precipitation agent adopted is acetone, and the volume ratio of described dilute sulphuric acid and precipitation agent is 1:1-1:2.5.
6. the method utilizing containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid and vitriol according to claim 1, the vitriol obtained after it is characterized in that described solid-liquid separation adopts described precipitation agent to be that washing composition repeatedly washs, until washing after filtrate in sulfuric acid massfraction content lower than 0.5%, again carry out solid-liquid separation afterwards, obtain required sulfate product.
7. the method for containing sulfate dilute sulphuric acid reclaim(ed) sulfuric acid according to claim 6 and vitriol, it is characterized in that described dilute sulphuric acid filtrate adopts air distillation to reclaim and obtains partly precipitated agent, dilute sulphuric acid remaining after distillation adopts underpressure distillation vacuum concentration to obtain the vitriol oil.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107417307A (en) * | 2017-09-12 | 2017-12-01 | 化工部长沙设计研究院 | A kind of preparation technology of water-soluble drip irrigation potassium sulfate |
| CN108330298A (en) * | 2018-02-14 | 2018-07-27 | 中南大学 | A method of extracting rubidium, caesium, lithium, potassium from more metal mica ores |
| CN109179745A (en) * | 2018-08-29 | 2019-01-11 | 杭州轩辉环境设备有限公司 | A kind for the treatment of process for the waste water producing fatty acid generation |
| CN109231399A (en) * | 2018-08-28 | 2019-01-18 | 杭州轩辉环境设备有限公司 | A kind of process for extracting sulfate |
| CN109824021A (en) * | 2019-04-15 | 2019-05-31 | 新疆大学 | A kind of method of industrial waste sulfuric acid circular regeneration |
| CN110451463A (en) * | 2019-09-06 | 2019-11-15 | 攀枝花学院 | The method for removing iron of titanium dioxide waste acid by sulfuric acid process |
| CN114540620A (en) * | 2022-02-22 | 2022-05-27 | 桐乡市思远环保科技有限公司 | Method for removing sulfate in chloride leaching process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0363683A1 (en) * | 1988-09-26 | 1990-04-18 | Sulzer Chemtech AG | Process for the recovery of greatly concentrated sulfuric-acid solutions by the treatment of diluted sulfate-containing sulfuric-acid concentrations |
| CN1760117A (en) * | 2005-10-19 | 2006-04-19 | 兰州大学 | Method for recovering vitriol from waste vitrol containing metal salt |
-
2015
- 2015-06-02 CN CN201510294930.7A patent/CN104876194A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0363683A1 (en) * | 1988-09-26 | 1990-04-18 | Sulzer Chemtech AG | Process for the recovery of greatly concentrated sulfuric-acid solutions by the treatment of diluted sulfate-containing sulfuric-acid concentrations |
| CN1760117A (en) * | 2005-10-19 | 2006-04-19 | 兰州大学 | Method for recovering vitriol from waste vitrol containing metal salt |
Non-Patent Citations (3)
| Title |
|---|
| 王和庆: ""溶析结晶法脱除钛白废酸中硫酸亚铁盐的研究"", 《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》 * |
| 王建成: ""有机溶剂析出法结晶分离水溶液中的硫酸钾"", 《山东轻工业学院学报》 * |
| 郭雨 等: ""乙醇溶析结晶法从白炭黑废母液中回收硫酸钠"", 《化工环保》 * |
Cited By (9)
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| CN107417307A (en) * | 2017-09-12 | 2017-12-01 | 化工部长沙设计研究院 | A kind of preparation technology of water-soluble drip irrigation potassium sulfate |
| CN107417307B (en) * | 2017-09-12 | 2020-11-06 | 化工部长沙设计研究院 | Preparation process of potassium sulfate for water-soluble drip irrigation |
| CN108330298A (en) * | 2018-02-14 | 2018-07-27 | 中南大学 | A method of extracting rubidium, caesium, lithium, potassium from more metal mica ores |
| CN108330298B (en) * | 2018-02-14 | 2020-08-25 | 中南大学 | Method for extracting rubidium, cesium, lithium and potassium from polymetallic mica ore |
| CN109231399A (en) * | 2018-08-28 | 2019-01-18 | 杭州轩辉环境设备有限公司 | A kind of process for extracting sulfate |
| CN109179745A (en) * | 2018-08-29 | 2019-01-11 | 杭州轩辉环境设备有限公司 | A kind for the treatment of process for the waste water producing fatty acid generation |
| CN109824021A (en) * | 2019-04-15 | 2019-05-31 | 新疆大学 | A kind of method of industrial waste sulfuric acid circular regeneration |
| CN110451463A (en) * | 2019-09-06 | 2019-11-15 | 攀枝花学院 | The method for removing iron of titanium dioxide waste acid by sulfuric acid process |
| CN114540620A (en) * | 2022-02-22 | 2022-05-27 | 桐乡市思远环保科技有限公司 | Method for removing sulfate in chloride leaching process |
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