CN105368476A - Asphalt extraction technological process by mineral asphalt solvent - Google Patents
Asphalt extraction technological process by mineral asphalt solvent Download PDFInfo
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- CN105368476A CN105368476A CN201510786375.XA CN201510786375A CN105368476A CN 105368476 A CN105368476 A CN 105368476A CN 201510786375 A CN201510786375 A CN 201510786375A CN 105368476 A CN105368476 A CN 105368476A
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Abstract
The invention relates to the technical field of asphalt production, especially an asphalt extraction technological process by a mineral asphalt solvent. The process comprises the following steps: S1: raw material pretreatment, S2: drying, S3: blending and feeding, S4: solvent extraction, S5: asphalt oil and ore separation, S6: sandstone processing and recycling, S7: mixed oil filtration, S8: separation and recovery of asphalt oil and the solvent, S9: solvent evaporation and condensation recovery, and S10: tail gas recovery. The method uses the different initial boiling points and distillation points of the solvent and the asphalt oil, so the solvent is evaporated before the boiling point of the asphalt oil is met; and then the gasified solvent is cooled and recycled, so as to reduce the cost.
Description
Technical field
The present invention relates to asphalt production technical field, particularly a kind of ore deposit asphalt flux extraction asphalter process flow.
Background technology
Pitch is extract asphalt oil by solvent in the process of actual production, but people often only carry out the extraction of 1 to 2 times to asphalite, result in asphalite oil yield low, thus cause great loss; And along with the consumption of the continuous leaching solvent of asphalt oil also can be very large, thus inversion production cost constantly raises.So need to carry out recycling to solvent to reduce production cost, solvent is extracted from mixing oil, utilize the different of the initial boiling point destructive distillation point of solvent and asphalt oil, heat up in a steamer a little not reaching asphalt oil, solvent is first evaporated, then cooling collection is carried out to vaporized solvent, thus play the effect reduced costs.
Summary of the invention
Technical purpose of the present invention is the different of initial boiling point destructive distillation point by utilizing solvent and asphalt oil, heats up in a steamer a little and first evaporates solvent not reaching asphalt oil, then carry out cooling to vaporized solvent and reclaim, thus play the effect reduced costs; A kind of ore deposit asphalt flux extraction asphalter process flow is provided.
For solving above-mentioned technical problem, a kind of ore deposit asphalt flux that provides of the present invention extracts asphalter process flow, and it comprises the following steps:
S1: raw materials pretreatment: solid for ore deposit asphalt material block is carried out just broken, the ore deposit asphalt material after fragmentation is sieved, distinguishes coarse fodder and fines, and remove foreign matter;
S2: dry: reduce and the water ratio controlled in the asphalt material of ore deposit by heating;
S3: blending feeding: coarse fodder and fines or fines and stone are carried out mix at reactor in proportion;
S4: solvent extraction: utilize solvent to carry out drip washing to the batching mixed in step S3 in reactor, leaches asphalt oil and forms mixing oil solution (asphalt oil and solvent), can produce tail gas in the process of extraction;
S5: asphalt oil is separated with ore in sand form: mixing oil solution (asphalt oil and solvent) is separated with ore in sand form by solid-liquid separator;
S6: sandstone disposal and recovery: the ore in sand form sieved out in step S5 is carried out successively stir, broken, dry, clean and screening, solvent remaining on ore in sand form is recycled by the mode of evaporating;
S7: mixing oil filtration: filter the mixing oil solution sieved out in step S5 (asphalt oil and solvent), removes the micro-ore in sand form in mixing oil solution (asphalt oil and solvent);
S8: asphalt oil is separated and recovery from solvent: utilize the initial boiling point of asphalt oil and solvent, destructive distillation point different, by vaporizer, the mixing oil solution (asphalt oil and solvent) after step S7 filtration is evaporated, make the solvent words said in a fit of rage, thus asphalt oil is separated completely with solvent;
S9: solvent evaporation is reclaimed with condensation: cooled by the solvent evaporated in step S6 and step S8, then reclaimed solvent by water-and-oil separator, meeting tail gas after cooling;
S10: tail gas recycle: tail gas in step S4 and step S9 is carried out unify process, discharge again after making it reach standard.
Further: in described step S1, the grain size specification of coarse fodder is 10-20mm, the grain size specification of fines is below 10mm.
Further again: in described step S2 by the moisture control in the asphalt material of ore deposit at 2-4%.
Further again: in described step S3, the proportioning of coarse fodder and fines is 1:1, the proportioning of described fines and stone is 1:1.5.
Further again: described step S4: solvent extraction carries out continuous four extractions at reactor, and first three extraction is carried out at normal temperatures, and the temperature of the 4th extraction controls at 50-55 DEG C, and the time of four extractions is all 15min.
Further again: the bake out temperature in described step S5 controls at about 105-115 DEG C.
Further again: the vaporization temperature in described step S8 controls 110 DEG C.
Adopt after aforesaid method, the present invention, by utilizing the different of the initial boiling point destructive distillation point of solvent and asphalt oil, heats up in a steamer a little and first evaporates solvent not reaching asphalt oil, then carry out cooling recovery to vaporized solvent, thus play the effect reduced costs; And the oil yield of asphalite is improved by four extractions, reduce unnecessary loss.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.
Fig. 1 is process flow sheet of the present invention.
Embodiment
The invention provides a kind of ore deposit asphalt flux extraction asphalter process flow, it comprises the following steps:
S1: raw materials pretreatment: solid for ore deposit asphalt material block is carried out just broken, the ore deposit asphalt material after fragmentation is sieved, distinguishes coarse fodder and fines, and remove foreign matter;
S2: dry: reduce and the water ratio controlled in the asphalt material of ore deposit by heating;
S3: blending feeding: coarse fodder and fines or fines and stone are carried out mix at reactor in proportion;
S4: solvent extraction: utilize solvent to carry out drip washing to the batching mixed in step S3 in reactor, leaches asphalt oil and forms mixing oil solution (asphalt oil and solvent), can produce tail gas in the process of extraction;
S5: asphalt oil is separated with ore in sand form: mixing oil solution (asphalt oil and solvent) is separated with ore in sand form by solid-liquid separator;
S6: sandstone disposal and recovery: the ore in sand form sieved out in step S5 is carried out successively stir, broken, dry, clean and screening, solvent remaining on ore in sand form is recycled by the mode of evaporating;
S7: mixing oil filtration: filter the mixing oil solution sieved out in step S5 (asphalt oil and solvent), removes the micro-ore in sand form in mixing oil solution (asphalt oil and solvent);
S8: asphalt oil is separated and recovery from solvent: utilize the initial boiling point of asphalt oil and solvent, destructive distillation point different, by vaporizer, the mixing oil solution (asphalt oil and solvent) after step S7 filtration is evaporated, make the solvent words said in a fit of rage, thus asphalt oil is separated completely with solvent;
S9: solvent evaporation is reclaimed with condensation: cooled by the solvent evaporated in step S6 and step S8, then reclaimed solvent by water-and-oil separator, meeting tail gas after cooling;
S10: tail gas recycle: tail gas in step S4 and step S9 is carried out unify process, discharge again after making it reach standard.
In above-mentioned step S1, the grain size specification of coarse fodder is 10-20mm, and the grain size specification of fines is below 10mm.
In above-mentioned step S2 by the moisture control in the asphalt material of ore deposit at 2-4%.
In above-mentioned step S3, the proportioning of coarse fodder and fines is 1:1, and the proportioning of described fines and stone is 1:1.5.Object: when infiltrating extraction pitch with solvent, because fines is many, after asphalt oil is extracted, fine granularity mineral aggregate can be cracked into particulate fine sand by nature, cause feed liquid contact area relatively little, easy closely knit precipitation during infiltration, not only weaken the seepage force of solvent, and cause pitch fully not leach, after extraction, residue Draining time is long simultaneously, this auxiliary process is by the clean stone (particle diameter is 15mm) of blending 1:1 or 1:1.5 ratio, or 20--10mm coarse fodder, form " cellular " compound, increase feed liquid contact area, strengthen the ability of the solvent penetration bed of material, secondary solvent extraction pitch amount, and stone and solvent reactionless, do not affect any physics of extract, chemical property, stone is in whole equipment runs simultaneously, almost without physics consumption, stone is recyclable, stone and slag is reclaimed by screening after extraction.
Above-mentioned step S4: solvent extraction carries out continuous four extractions at reactor, first three extraction is carried out at normal temperatures, the temperature of the 4th extraction controls at 50-55 DEG C, the time of four extractions is all 15min, after first three extraction, the oil yield of asphalt oil reaches 30%, and after the 4th extraction, the oil yield of asphalt oil reaches 80 ~ 85%.
Bake out temperature in above-mentioned step S5 controls at about 105-115 DEG C.
If in above-mentioned step S7 when containing micro-ore in sand form in mixing oil solution (asphalt oil and solvent), it will not only affect the quality of extraction pitch, and very easily damage mixing oil transferpump, therefore must filter before mixing oil carries out asphalt oil and recycled solvent.
Vaporization temperature in above-mentioned step S8 controls 110 DEG C.Heating up in a steamer of this solvent is some 60--90 DEG C, be heated to 110 DEG C, solvent energy 100% reclaims, heating up in a steamer of asphalt stock fore-running is a little 200 ~ 250 DEG C, 30 ~ 250 DEG C or 250 ~ 300 DEG C, mixing oil after filtration is admitted to vaporizer, being heated to 110 DEG C makes solvent in mixing oil be evaporated by 100%, thus asphalt oil is all separated with solvent.
Claims (7)
1. an ore deposit asphalt flux extraction asphalter process flow, is characterized in that: comprise the following steps:
S1: raw materials pretreatment: solid for ore deposit asphalt material block is carried out just broken, the ore deposit asphalt material after fragmentation is sieved, distinguishes coarse fodder and fines, and remove foreign matter;
S2: dry: reduce and the water ratio controlled in the asphalt material of ore deposit by heating;
S3: blending feeding: coarse fodder and fines or fines and stone are carried out mix at reactor in proportion;
S4: solvent extraction: utilize solvent to carry out drip washing to the batching mixed in step S3 in reactor, leaches asphalt oil and forms mixing oil solution (asphalt oil and solvent), can produce tail gas in the process of extraction;
S5: asphalt oil is separated with ore in sand form: mixing oil solution (asphalt oil and solvent) is separated with ore in sand form by solid-liquid separator;
S6: sandstone disposal and recovery: the ore in sand form sieved out in step S5 is carried out successively stir, broken, dry, clean and screening, solvent remaining on ore in sand form is recycled by the mode of evaporating;
S7: mixing oil filtration: filter the mixing oil solution sieved out in step S5 (asphalt oil and solvent), removes the micro-ore in sand form in mixing oil solution (asphalt oil and solvent);
S8: asphalt oil is separated and recovery from solvent: utilize the initial boiling point of asphalt oil and solvent, destructive distillation point different, by vaporizer, the mixing oil solution (asphalt oil and solvent) after step S7 filtration is evaporated, make the solvent words said in a fit of rage, thus asphalt oil is separated completely with solvent;
S9: solvent evaporation is reclaimed with condensation: cooled by the solvent evaporated in step S6 and step S8, then reclaimed solvent by water-and-oil separator, meeting tail gas after cooling;
S10: tail gas recycle: tail gas in step S4 and step S9 is carried out unify process, discharge again after making it reach standard.
2. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, it is characterized in that: in described step S1, the grain size specification of coarse fodder is 10-20mm, the grain size specification of fines is below 10mm.
3. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, is characterized in that: in described step S2 by the moisture control in the asphalt material of ore deposit at 2-4%.
4. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, it is characterized in that: in described step S3, the proportioning of coarse fodder and fines is 1:1, the proportioning of described fines and stone is 1:1.5.
5. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, it is characterized in that: described step S4: solvent extraction carries out continuous four extractions at reactor, first three extraction is carried out at normal temperatures, the temperature of the 4th extraction controls at 50-55 DEG C, and the time of four extractions is all 15min.
6. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, is characterized in that: the bake out temperature in described step S5 controls at about 105-115 DEG C.
7. a kind of ore deposit according to claim 1 asphalt flux extraction asphalter process flow, is characterized in that: the vaporization temperature in described step S8 controls 110 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510786375.XA CN105368476A (en) | 2015-11-16 | 2015-11-16 | Asphalt extraction technological process by mineral asphalt solvent |
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| CN201510786375.XA CN105368476A (en) | 2015-11-16 | 2015-11-16 | Asphalt extraction technological process by mineral asphalt solvent |
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| CN105368476A true CN105368476A (en) | 2016-03-02 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054885A (en) * | 2018-08-30 | 2018-12-21 | 山东宜水新材料科技有限公司 | A kind of oil-sand selectivity fractional extraction technique |
| CN109260755A (en) * | 2018-09-27 | 2019-01-25 | 凌港 | The separation method of highway waste asphalt pavement material |
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| CA2738194A1 (en) * | 2011-04-27 | 2012-10-27 | Imperial Oil Resources Limited | Method of processing a bituminous feed using an emulsion |
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| CN103693833A (en) * | 2012-09-28 | 2014-04-02 | 中国石油天然气股份有限公司 | Comprehensive control method of oily sludge |
| CN104449785A (en) * | 2014-10-23 | 2015-03-25 | 宁波博汇化工科技股份有限公司 | Deashing processing technique for natural asphalt |
| CN204439433U (en) * | 2015-02-03 | 2015-07-01 | 中国海洋石油总公司 | The centrifugal bitumen extractor of a kind of fully automatic roll type |
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2015
- 2015-11-16 CN CN201510786375.XA patent/CN105368476A/en active Pending
Patent Citations (7)
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| CN202099246U (en) * | 2011-03-31 | 2012-01-04 | 张靖 | Natural rock asphalt purification device |
| CA2738194A1 (en) * | 2011-04-27 | 2012-10-27 | Imperial Oil Resources Limited | Method of processing a bituminous feed using an emulsion |
| JP3172746U (en) * | 2011-10-21 | 2012-01-05 | 株式会社 ナカジマ技販 | Rotary asphalt extraction equipment |
| CN103693833A (en) * | 2012-09-28 | 2014-04-02 | 中国石油天然气股份有限公司 | Comprehensive control method of oily sludge |
| CN203360383U (en) * | 2013-06-16 | 2013-12-25 | 李永杰 | Waste asphalt reclaiming system |
| CN104449785A (en) * | 2014-10-23 | 2015-03-25 | 宁波博汇化工科技股份有限公司 | Deashing processing technique for natural asphalt |
| CN204439433U (en) * | 2015-02-03 | 2015-07-01 | 中国海洋石油总公司 | The centrifugal bitumen extractor of a kind of fully automatic roll type |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054885A (en) * | 2018-08-30 | 2018-12-21 | 山东宜水新材料科技有限公司 | A kind of oil-sand selectivity fractional extraction technique |
| CN109260755A (en) * | 2018-09-27 | 2019-01-25 | 凌港 | The separation method of highway waste asphalt pavement material |
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| CB03 | Change of inventor or designer information |
Inventor after: Yang Zaisheng Inventor after: Gong Lixin Inventor after: Wu Jiehao Inventor after: Dan Donghao Inventor after: Su Chaohui Inventor after: Luo Shi Inventor before: Yang Zaisheng Inventor before: Gong Lixin Inventor before: Wu Jiehao Inventor before: Dan Donghao |
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| COR | Change of bibliographic data | ||
| PB01 | Publication | ||
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| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160302 |