CN103496684A - Rapid heating extraction method of extraction tank - Google Patents
Rapid heating extraction method of extraction tank Download PDFInfo
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- CN103496684A CN103496684A CN201310413926.9A CN201310413926A CN103496684A CN 103496684 A CN103496684 A CN 103496684A CN 201310413926 A CN201310413926 A CN 201310413926A CN 103496684 A CN103496684 A CN 103496684A
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- extraction
- extraction tank
- phosphoric acid
- tank
- ore pulp
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Abstract
The invention discloses a rapid heating extraction method of an extraction tank. The method comprises the steps: (1) after the extraction tank is cleared, complementing dilute phosphoric acid to a 1.5m position in the extraction tank; (2) starting stirring fans and tail gas fans in all regions, and keeping the extraction tank at micro-negative pressure; (3) respectively adding sulfuric acid and phosphoric ore pulp into the extraction tank at the speeds of 3m<3>/h and 5m<3>/h, heating and thickening, wherein the dilute phosphoric acid or sewage is complemented again into the heating process so that the liquid level of the extraction tank and the proportion of the extracted phosphoric acid are controlled; (4) when the extraction temperature is up to 60 DEG C, adjusting the negative pressure value of each tail gas fan, gradually increasing the adding amounts of the sulfuric acid and the phosphoric ore pulp, and shortening the heating and thickening times of the extraction tank; and (5) when the liquid level and all indexes of the extraction tank meet a filtrations condition, filtering and washing, collecting solids into a gypsum stockpile, collecting liquid into a phosphoric acid tank, and exhausting tail gas after the tail gas is washed and emptied by using a washing tower. The rapid heating extraction method has the advantages that the heating and thickening times are saved, reducing the production costs of enterprises is reduced, extraction reaction effect is good and the like.
Description
Technical field
The present invention relates to a kind of the be rapidly heated method of extraction of extraction tank, relate in particular in a kind of industrial production the phosphoric acid extraction extracting process that is rapidly heated.
Background technology
At present, in process to extraction tank fouling cleaning, in order to ensure the stable control of percentage extraction, formulated the extraction tank cleaning cycle, the annual need cleared up extraction tank 3-4 time, each extraction tank of having cleared up, need be to supplementing the light phosphoric acid of part and sewage in extraction tank, in extraction tank, temperature, in 30 degree left and right, need add steam to be heated up, when temperature increase to 60 is spent, to extraction tank, add again a small amount of sulfuric acid and phosphate ore pulp to heat up and put forward phosphoric acid extraction concentration.But many containing condensation water quantity in steam, entering of a large amount of water of condensation in temperature-rise period in steam one is to reduce phosphoric acid extraction proportion, the 2nd, increased the extraction tank liquid level, cause phosphoric acid extraction proportion in extraction tank intensification concentrate process to hang down with liquid-solid ratio low, extraction tank intensification concentrate needs to complete in nearly more than 20 hours, during extraction tank intensification concentrate, the at most effective usage quantity of phosphoric acid stock is at 800m
3, the compound fertilizer system is per hour used phosphatase 24 0m
3, extraction tank is put forward liquid-solid ratio and is carried light phosphoric acid and maintenance clearance time also to need about 16 hours.So the extraction tank heating-up time is long, can force the compound fertilizer system shift to an earlier date decrement production and cause damp production.
Summary of the invention
The defect and the problem that in order to overcome above-mentioned prior art, exist, a kind of method that the object of the present invention is to provide extraction tank to be rapidly heated and to extract.
The technical scheme of employing of the present invention is:
A kind of method that extraction tank is rapidly heated and extracts, concrete steps are:
1), after extraction tank cleans out, fill into the light phosphoric acid of 1～19% concentration to the interior 1.5m of extraction tank place;
2) open each district of extraction tank and stir and extraction tank tail gas induced draft fan, extraction tank keeps micro-negative pressure 300-500pa;
3) with 3m
3the speed of/h and with 5m
3the speed of/h is respectively toward the phosphate ore pulp intensification concentrate that adds sulfuric acid and the phosphorus content 29% of 93% concentration in extraction tank, and the bulk specific gravity of sulfuric acid and phosphate ore pulp is 1:1.5～1.6, SO during interpolation
3the span of control of concentration index is 0.025-0.040g/ml; In temperature-rise period, by the light phosphoric acid that fills into 1～19% concentration or the sewage of clearing up the filtering system generation, control extraction tank liquid level and phosphoric acid extraction proportion;
4) when extraction temperature arrival 60 is spent, regulate exhaust fan negative pressure amount 800～1500pa, increase sulfuric acid and phosphate ore pulp add-on, its speed is respectively: sulfuric acid 3-13m
3/ h and phosphate ore pulp 5-24m
3/ h;
5) carry out filtration washing after 8 hours, solid collection is to the gypsum storehouse, and liquid collecting is in the phosphoric acid tank, and tail gas is by the emptying rear discharge of washing tower washing.
The described extraction tank liquid level of step 3) is less than 3.5m.
The described phosphoric acid extraction proportion of step 3) is 1.23-1.27g/cm
3.
Beneficial effect of the present invention: 1, this working method concentrate time of not only heating up fast, and extractive reaction is effective.2, saved the intensification concentrate time, improved driving rate.3, do not use steam to heat up, reduced company's production cost.
The accompanying drawing explanation
Fig. 1 is method artwork of the present invention;
Embodiment
1 the present invention is further illustrated with reference to the accompanying drawings.
Embodiment 1
As Fig. 1, shown extraction tank, after extraction tank cleans out, fill into the light phosphoric acid of 1～19% concentration of 140 cubic metres to 1.5m place in extraction tank, opens extraction tank each district's stirring and exhaust fan, and extraction tank keeps micro-negative pressure 300pa, with 3m
3the speed of/h and with 5m
3the speed of/h is respectively toward the phosphate ore pulp intensification concentrate that adds sulfuric acid and the phosphorus content 29% of 93% concentration in extraction tank, and the bulk specific gravity of sulfuric acid and phosphate ore pulp is 1:1.6, analyzes liquid phase SO
3concentration value, draw SO
3concentration is 0.020g/ml, increases sulfuric acid and adds speed to arrive 5m
3/ h, SO
3when concentration is 0.028g/ml, it is 3m that readjustment sulfuric acid adds speed
3/ h; Now phosphoric acid extraction proportion is 1.20g/cm
3, add 1～19% the light phosphoric acid of 80 cubic metres, make phosphoric acid extraction proportion obtain 1.26g/cm
3, the extraction tank liquid level is 2.6m.
When extraction temperature arrival 60 is spent, regulate exhaust fan negative pressure amount 800pa, with 13m
3/ h and 5m
3the speed of/h progressively adds sulfuric acid and phosphate ore pulp, carries out filtration washing after 8 hours, phosphoric acid hourly output 36m
3; Tail gas is emptying through washing tower and chimney, produces slip and separates through filter, and the solid transfer of gained is to the gypsum storehouse, and liquid makes phosphoric acid to the phosphoric acid tank.
Embodiment 2
After extraction tank cleans out, fill into the light phosphoric acid of 1～19% concentration of 140 cubic metres to 1.5m place in extraction tank, open extraction tank each district's stirring and exhaust fan, extraction tank keeps micro-negative pressure 500pa, with 3m
3the speed of/h and with 5m
3the speed of/h is respectively toward the phosphate ore pulp intensification concentrate that adds sulfuric acid and the phosphorus content 29% of 93% concentration in extraction tank, and the bulk specific gravity of sulfuric acid and phosphate ore pulp is 1:1.5, analyzes liquid phase SO
3concentration value, draw SO
3concentration is 0.036g/ml; Phosphoric acid extraction proportion is 1.28g/cm
3, the sewage that adds the cleaning filtering system of 50 cubic metres to produce, make phosphoric acid extraction proportion at 1.23g/cm
3, the extraction tank liquid level is in 2.9m.
When extraction temperature arrival 60 is spent, regulate exhaust fan negative pressure amount 1500pa, with 10m
3/ h and 10m
3the speed of/h progressively adds sulfuric acid and phosphate ore pulp, carries out filtration washing after 8 hours, phosphoric acid hourly output 40m
3; Tail gas is emptying through washing tower and chimney, produces slip and separates through filter, and the solid transfer of gained is to the gypsum storehouse, and liquid makes phosphoric acid to the phosphoric acid tank.
Embodiment 3
As Fig. 1, shown extraction tank, after extraction tank cleans out, fill into the light phosphoric acid of 1～19% concentration of 140 cubic metres to 1.5m place in extraction tank, opens extraction tank each district's stirring and exhaust fan, and extraction tank keeps micro-negative pressure 400pa, with 3m
3the speed of/h and with 5m
3the speed of/h is respectively toward the phosphate ore pulp intensification concentrate that adds sulfuric acid and the phosphorus content 29% of 93% concentration in extraction tank, and the bulk specific gravity of sulfuric acid and phosphate ore pulp is 1:1.5, analyzes liquid phase SO
3concentration value, draw SO
3concentration is 0.021g/ml, increases sulfuric acid and adds speed to arrive 5m
3/ h, SO
3when concentration is 0.029g/ml, it is 3m that readjustment sulfuric acid adds speed
3/ h; Now phosphoric acid extraction proportion is 1.20g/cm
3, add 1～19% the light phosphoric acid of 80 cubic metres, make phosphoric acid extraction proportion obtain 1.27g/cm
3, the extraction tank liquid level is 2.4m.
When extraction temperature arrival 60 is spent, regulate exhaust fan negative pressure amount 1000pa, with 3m
3/ h and 24m
3the speed of/h progressively adds sulfuric acid and phosphate ore pulp, carries out filtration washing after 8 hours, phosphoric acid hourly output 39m
3; Tail gas is emptying through washing tower and chimney, produces slip and separates through filter, and the solid transfer of gained is to the gypsum storehouse, and liquid makes phosphoric acid to the phosphoric acid tank.
Claims (3)
1. the method that extraction tank is rapidly heated and extracts, is characterized in that, concrete steps are:
1), after extraction tank cleans out, fill into the light phosphoric acid of 1～19% concentration to the interior 1.5m of extraction tank place;
2) open each district of extraction tank and stir and extraction tank tail gas induced draft fan, extraction tank keeps micro-negative pressure 300-500pa;
3) with 3m
3the speed of/h and with 5m
3the speed of/h adds the sulfuric acid of 93% concentration and the phosphate ore pulp intensification concentrate that phosphorus content is 29% respectively in extraction tank, and the bulk specific gravity of sulfuric acid and phosphate ore pulp is 1:1.5～1.6, SO during interpolation
3the span of control of concentration index is 0.025-0.040g/ml; In temperature-rise period, by the light phosphoric acid that fills into 1～19% concentration or the sewage of clearing up the filtering system generation, control extraction tank liquid level and phosphoric acid extraction proportion;
4) when extraction temperature arrival 60 is spent, regulate exhaust fan negative pressure amount 800～1500pa, progressively increase sulfuric acid and phosphate ore pulp add-on, its speed is respectively: sulfuric acid 3-13m
3/ h and phosphate ore pulp 5-24m
3/ h;
5) carry out filtration washing after 8 hours, solid collection is to the gypsum storehouse, and liquid collecting is in the phosphoric acid tank, and tail gas is by the emptying rear discharge of washing tower washing.
2. the method for claim 1, it is characterized in that: the described tank liquor position of taking of step 3) is less than 3.5m.
3. the method for claim 1, it is characterized in that: the described phosphoric acid extraction proportion of step 3) is 1.23-1.27g/cm
3.
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|---|---|---|---|
| CN201310413926.9A CN103496684B (en) | 2013-09-12 | 2013-09-12 | Rapid heating extraction method of extraction tank |
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|---|---|---|---|
| CN201310413926.9A CN103496684B (en) | 2013-09-12 | 2013-09-12 | Rapid heating extraction method of extraction tank |
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| CN103496684A true CN103496684A (en) | 2014-01-08 |
| CN103496684B CN103496684B (en) | 2015-06-17 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113073200A (en) * | 2021-04-07 | 2021-07-06 | 广东明方科技有限公司 | Waste circuit board copper metal enrichment extraction device and extraction method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549346A (en) * | 2009-05-12 | 2009-10-07 | 瓮福（集团）有限责任公司 | A wet phosphoric acid purifying extractor descaling method |
| CN102390821A (en) * | 2011-08-08 | 2012-03-28 | 云南云天化国际化工股份有限公司 | Method for producing dihydrate wet-process phosphoric acid |
| CN102431981A (en) * | 2011-09-01 | 2012-05-02 | 贵州开磷（集团）有限责任公司 | Method for reducing SO3 concentration in diluted phosphoric acid |
-
2013
- 2013-09-12 CN CN201310413926.9A patent/CN103496684B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549346A (en) * | 2009-05-12 | 2009-10-07 | 瓮福（集团）有限责任公司 | A wet phosphoric acid purifying extractor descaling method |
| CN102390821A (en) * | 2011-08-08 | 2012-03-28 | 云南云天化国际化工股份有限公司 | Method for producing dihydrate wet-process phosphoric acid |
| CN102431981A (en) * | 2011-09-01 | 2012-05-02 | 贵州开磷（集团）有限责任公司 | Method for reducing SO3 concentration in diluted phosphoric acid |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113073200A (en) * | 2021-04-07 | 2021-07-06 | 广东明方科技有限公司 | Waste circuit board copper metal enrichment extraction device and extraction method thereof |
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| CN103496684B (en) | 2015-06-17 |
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Inventor after: Cai Yingqiang Inventor after: Sun Haibing Inventor after: Wang Guanghui Inventor after: Wei Maosong Inventor after: Yu Hai Inventor after: Xu Bin Inventor before: Sun Haibing Inventor before: Wang Guanghui Inventor before: Wei Maosong Inventor before: Yu Hai Inventor before: Xu Bin |