CN103509597A - Recycling processing method and processing system for waste oil - Google Patents
Recycling processing method and processing system for waste oil Download PDFInfo
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- CN103509597A CN103509597A CN201310299057.1A CN201310299057A CN103509597A CN 103509597 A CN103509597 A CN 103509597A CN 201310299057 A CN201310299057 A CN 201310299057A CN 103509597 A CN103509597 A CN 103509597A
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Abstract
The invention provides a recycling processing method and processing system for waste oil. The key for the processing method is cycling repeated flash evaporation, which comprises preheating raw oil, directly sending the raw oil into a high temperature circulating system for the cycling repeated flash reaction to crack the raw oil into gas, carrying out subsequent catalytic reaction on gas to obtain mixed crude oil and carrying out fractionation on the mixed crude oil, and flowing the uncracked raw oil back into the high temperature circulating system for continuing the cycling repeated flash evaporation reaction and generating gas. The key for the processing system lies in a high temperature cycling system composed of a high temperature circulating pump, a circulating pipeline and a primary fractionation tower. The method provided by the invention has the advantages of simple operation and high processing efficiency, and the processing system has the advantages of simple device and high reliability. The whole recovery process does not produce waste oil, which cannot be processed, so as to avoid waste and play a positive role in protection of the environment.
Description
Technical field
The present invention relates to a kind of waste oil recovery and treatment method and treatment system, provide specifically a kind of gasoline, diesel oil, lubricated wet goods usable oils are processed and formed to used oil, heavy oil or plastics wet goods waste oil by the method for the flash distillation repeatedly that circulates and the treatment system of stove three towers.
Background technology
At present, China only motor vehicle, ship and mechanical means and all kinds of machine oil that consume over 7,000,000 tons, nearly 6,000,000 tons of the waste oil producing, these waste oil great majority be used as oil fuel with by illegal retailer and enterprise with inferior quality, poor efficiency refine into vapour, diesel oil comes into the market.Owing to mostly containing poisonous and hazardous material in waste oil, the as easy as rolling off a log pollution that causes environment of above-mentioned treatment process.And some underground little refinerys, from Auto repair shop or 4 S auto shop, buy waste oil and through Indigenous Smelting Method, make vapour, diesel oil again, be then sold to oil depot or service station, be in harmonious proportion laggard marketing with good processed oil and sell, adulterate, serious harm the safe operation of equipment and vehicle.
Cause the major cause of existing waste oil treatment confusion to be to lack efficient and waste oil recovery and treatment method and treatment system cheaply, therefore develop a kind of new waste oil recovery and treatment method and treatment system just seems extremely important.
Summary of the invention
It is low that the present invention mainly solves existing waste oil treatment system processing efficiency, the problem that cost is higher, a kind of new waste oil recovery and treatment method and treatment system are provided, and wherein the key of waste oil recovery and treatment method is the flash distillation repeatedly that circulates, and the key for the treatment of system is high temperature circulation system.
Waste oil recovery and treatment method provided by the invention, comprises the steps:
1) preheating material oil;
2) stock oil after preheating is sent in high temperature circulation system and heated and the flash distillation scission reaction repeatedly that circulates, stock oil cracking is become to gas and cracking stock oil;
3) gas and the oil of cracking stock not through just divide a tower carry out separated after, cracking stock oil does not pass back into the high temperature circulation system flash distillation scission reaction repeatedly of proceeding to circulate, gas enter into catalytic tower carry out forming after catalyzed reaction contain gasoline, diesel oil is slightly oily with mixing of heavy oil;
4) the thick oil of mixing is carried out to fractionation, and reclaim gasoline, diesel oil and heavy oil according to different cut points.
The key of the method is exactly the flash distillation repeatedly that circulates, after being preheating material oil, directly be sent to the circulate flash distillation repeatedly reaction of high temperature circulation system, at described circulation flash distillation scission reaction repeatedly Raw oil, continue cracking and become gas, uncracked stock oil is by just dividing a tower to carry out separated with gas, uncracked stock oil passes back into the high temperature circulation system flash distillation scission reaction repeatedly of proceeding to circulate, gas enters catalytic tower and carries out catalyzed reaction formation gasoline, diesel oil is slightly oily with mixing of heavy oil, mix thick oil and carry out fractionation, according to different cut points, reclaim gasoline, diesel oil and heavy oil.
Further, the temperature of preheating material oil is 150 ℃ to 200 ℃.
Further, the circulate Heating temperature of flash distillation scission reaction is repeatedly 320 ℃ to 420 ℃.
The present invention also provides the treatment system of utilizing aforesaid method, comprising:
Fuel oil preheating system, high temperature circulation system, catalytic reaction system and fractionating system, described fuel oil preheating system, high temperature circulation system, catalytic reaction system are connected in turn with fractionating system.
Further, described fuel oil preheating system comprises material tank, stock oil transferpump and process furnace, the top of described process furnace is provided with waste heat boiler, is respectively arranged with upper end pipeline opening and lower end pipeline opening in described waste heat boiler, is provided with the 3rd circulation line in described process furnace; Described material tank is connected with the input terminus of described stock oil transferpump by pipeline, and described stock oil carries delivery side of pump to be connected with the upper end pipeline opening of described waste heat boiler by pipeline.
Further, described high temperature circulation system comprises high temperature circulation transferpump and just divides tower, described high temperature circulation carries delivery side of pump to be connected by the first circulation line with the lower end of the 3rd circulation line, and the lower end pipeline opening of described waste heat boiler is connected with described the first circulation line by pipeline; The input terminus of described high temperature circulation transferpump is connected by the second circulation line with described Chu Fenta lower end, and the upper end of described the 3rd circulation line is connected with the described just tower body of minute tower by the 4th circulation line.
Further, described catalytic reaction system comprises catalytic tower, and described Chu Fenta upper end is connected with the tower body of described catalytic tower by pipeline.
Further, described fractionating system comprises separation column, end oil tank, gasoline tank and diesel oil oil tank, and the position that the upper end of described catalytic tower is connected with the tower body of described separation column by pipeline is consistent with the position that the tower body of described separation column is connected by pipeline with the lower end of described catalytic tower; The lower end of described separation column is connected with oil tank of the described end, the upper end of described separation column is connected with described gasoline tank, the side of the tower body of described separation column is provided with opening higher than the lower end of described separation column and lower than the upper end of described separation column, and described opening is connected with diesel oil oil tank by pipeline.
Further, described the 3rd circulation line is in a zigzag.
The key of this treatment system is to increase a high temperature circulation system between process furnace and catalytic tower, and this system is mainly by just dividing tower, high temperature circulation transferpump and high temperature circulation pipeline to form.By increasing high temperature circulation system, the continuous cracking of stock oil becomes gas, gas rises to first minute column overhead and enters into catalytic tower, uncracked stock oil reenters high temperature circulation pipeline, by high temperature circulation pump in circulating flash vaporization process repeatedly, thereby make the abundant cracking of stock oil become gas.
Waste oil recovery and treatment method provided by the present invention has to be implemented simply; processing efficiency advantages of higher; it is simple that treatment system has device; reliability high, because waste oil is always in circulation flash vaporization process, so guaranteed waste oil cracking fully; the rate of recovery is improved greatly; whole removal process can not produce not treatable waste oil, in the phenomenon that avoids waste, the protection of environment has also been played to positive effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet for the treatment of process of the present invention.
Fig. 2 is the one-piece construction schematic diagram for the treatment of system of the present invention.
Wherein 1 is material tank, and 2 is stock oil transferpump, and 3 is process furnace, 4 is waste heat boiler, and 5 is the 3rd circulation line, and 6 is high temperature circulation transferpump, 7 is the first circulation line, and 8 is the second circulation line, and 9 is just to divide tower, 10 is catalytic tower, 11 is separation column, and 12 is Fractionator Bottom oil tank, and 13 is diesel oil oil tank, 14 is gasoline tank, and 15 is the 4th circulation line.
Embodiment
For above-mentioned purpose of the present invention, feature and advantage can more be become apparent, below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.
Set forth detail in the following description so that fully understand the present invention.But the present invention can be different from alternate manner described here and implements with multiple, and those skilled in the art can do similar popularization without prejudice to intension of the present invention in the situation that.Therefore the present invention is not subject to the restriction of following public embodiment.
In conjunction with Fig. 1 and Fig. 2, stock oil is extracted out and is sent to from material tank 1 by stock oil transferpump 2 and in waste heat boiler 4, carries out preheating, preheating temperature can be 150 ℃ to 200 ℃ according to the difference of stock oil, stock oil after preheating enters into the first circulation line 7, because the first circulation line 7 is connected with the output terminal of high temperature circulation transferpump 6, therefore under pressure, the 3rd circulation line 5 that stock oil enters into process furnace 3 by the first circulation line 7 heats, Heating temperature is 320 ℃ to 420 ℃, by the 4th circulation line 15, entering into just minute tower 9, now a part of stock oil cracking becomes gas and at the beginning of rising to, divides the tower top of tower 9 to deliver into by the road catalytic tower 10, uncracked stock oil is reentering the first circulation line 7 by just dividing the second circulation line 8 of tower 9 lower ends to enter into high temperature circulation transferpump 6, do not stop to repeat above-mentioned circulation flash vaporization process repeatedly, because stock oil transferpump 2 can deliver into the recycle system by stock oil endlessly, therefore this working cycle can be sustained, the gas that enters into catalytic tower 10 carries out forming the thick oil of mixing after catalyzed reaction, mix the below that slightly oil enters into separation column 11 by Pipeline transport and carry out fractionation, according to the difference of cut point, obtain gasoline, diesel oil and end oil, gasoline delivers into gasoline tank 14, diesel oil delivers into diesel oil oil tank 13, and end oil delivers into Fractionator Bottom oil tank 12.
The present invention chooses used oil, useless heavy oil and plastic oil and as stock oil, by foregoing description method, tests respectively, and concrete outcome refers to following table:
By above table, can find out, the present invention is practical, and the rate of recovery is higher, has good market-oriented prospect.
Although the present invention with preferred embodiment openly as above; but it is not for limiting the present invention; any those skilled in the art without departing from the spirit and scope of the present invention; can utilize method and the technology contents of above-mentioned announcement to make possible change and modification to technical solution of the present invention; therefore; every content that does not depart from technical solution of the present invention; any simple modification, equivalent variations and the modification above embodiment done according to technical spirit of the present invention, all belong to the protection domain of technical solution of the present invention.
Claims (9)
1. a waste oil recovery and treatment method, is characterized in that, described method comprises the steps:
1) preheating material oil;
2) stock oil after preheating is sent in high temperature circulation system and heated and the flash distillation scission reaction repeatedly that circulates, stock oil cracking is become to gas and cracking stock oil;
3) gas and the oil of cracking stock not through just divide a tower carry out separated after, cracking stock oil does not pass back into the high temperature circulation system flash distillation scission reaction repeatedly of proceeding to circulate, gas enter into catalytic tower carry out forming after catalyzed reaction contain gasoline, diesel oil is slightly oily with mixing of heavy oil;
4) the thick oil of mixing is carried out to fractionation, and reclaim gasoline, diesel oil and heavy oil according to different cut points.
2. waste oil recovery and treatment method as claimed in claim 1, is characterized in that: in step 1), the temperature of stock oil is 150 ℃ to 200 ℃ described in preheating.
3. waste oil recovery and treatment method as claimed in claim 1, is characterized in that: in step 2) in, Heating temperature is 320 ℃ to 420 ℃.
4. a treatment system that is applied to the arbitrary described waste oil recovery and treatment method of claims 1 to 3, it is characterized in that, described system comprises: fuel oil preheating system, high temperature circulation system, catalytic reaction system and fractionating system, described fuel oil preheating system, high temperature circulation system, catalytic reaction system are connected in turn with fractionating system.
5. treatment system as claimed in claim 4, it is characterized in that: described fuel oil preheating system comprises material tank, stock oil transferpump and process furnace, the top of described process furnace is provided with waste heat boiler, in described waste heat boiler, be respectively arranged with upper end pipeline opening and lower end pipeline opening, in described process furnace, be provided with the 3rd circulation line; Described material tank is connected with the input terminus of described stock oil transferpump by pipeline, and described stock oil carries delivery side of pump to be connected with the upper end pipeline opening of described waste heat boiler by pipeline.
6. treatment system as claimed in claim 4, it is characterized in that: described high temperature circulation system comprises high temperature circulation transferpump and just divides tower, described high temperature circulation carries delivery side of pump to be connected by the first circulation line with the lower end of the 3rd circulation line, and the lower end pipeline opening of described waste heat boiler is connected with described the first circulation line by pipeline; The input terminus of described high temperature circulation transferpump is connected by the second circulation line with described Chu Fenta lower end, and the upper end of described the 3rd circulation line is connected with the described just tower body of minute tower by the 4th circulation line.
7. treatment system as claimed in claim 4, is characterized in that: described catalytic reaction system comprises catalytic tower, and described Chu Fenta upper end is connected with the tower body of described catalytic tower by pipeline.
8. treatment system as claimed in claim 4, it is characterized in that: described fractionating system comprises separation column, end oil tank, gasoline tank and diesel oil oil tank, the position that the upper end of described catalytic tower is connected with the tower body of described separation column by pipeline is consistent with the position that the tower body of described separation column is connected by pipeline with the lower end of described catalytic tower;
The lower end of described separation column is connected with oil tank of the described end, the upper end of described separation column is connected with described gasoline tank, the side of the tower body of described separation column is provided with opening higher than the lower end of described separation column and lower than the upper end of described separation column, and described opening is connected with diesel oil oil tank by pipeline.
9. treatment system as claimed in claim 5, is characterized in that: described the 3rd circulation line is in a zigzag.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310299057.1A CN103509597B (en) | 2013-07-17 | 2013-07-17 | Recycling processing method and processing system for waste oil |
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| CN201310299057.1A CN103509597B (en) | 2013-07-17 | 2013-07-17 | Recycling processing method and processing system for waste oil |
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| CN103509597A true CN103509597A (en) | 2014-01-15 |
| CN103509597B CN103509597B (en) | 2017-04-26 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105316033A (en) * | 2015-12-03 | 2016-02-10 | 南京绿帝环保能源科技有限公司 | Thermal cracking device for waste oil and waste engine oil |
| CN105441122A (en) * | 2015-12-18 | 2016-03-30 | 云南新昊环保科技有限公司 | Waste mineral oil cycle flash evaporation catalytic cracking recovery process |
| CN105567309A (en) * | 2015-12-18 | 2016-05-11 | 云南新昊环保科技有限公司 | Waste mineral oil circulating flash-evaporation catalytic cracking recovery plant |
| CN108048200A (en) * | 2018-01-30 | 2018-05-18 | 余永清 | Waste oil distills cracking and catalyzing system and production technology |
| CN108102681A (en) * | 2017-12-06 | 2018-06-01 | 菏泽万清源环保科技有限公司 | Hazardous waste resource regeneration method |
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| CN1434100A (en) * | 2003-03-10 | 2003-08-06 | 湖南大学 | Method for making fuel oil by mixing-cracking waste plastics, waste oil and heavy oil |
| RU2374299C2 (en) * | 2007-01-23 | 2009-11-27 | Геннадий Михайлович Яковлев | Method of advanced simultaneous processing liquid and solid hydrocarbon material and installation to this end |
| CN103087769A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Delayed coking method |
| CN203419889U (en) * | 2013-07-17 | 2014-02-05 | 上海顶丰能源科技有限公司 | Processing system for recycling waste oil |
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2013
- 2013-07-17 CN CN201310299057.1A patent/CN103509597B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1434100A (en) * | 2003-03-10 | 2003-08-06 | 湖南大学 | Method for making fuel oil by mixing-cracking waste plastics, waste oil and heavy oil |
| RU2374299C2 (en) * | 2007-01-23 | 2009-11-27 | Геннадий Михайлович Яковлев | Method of advanced simultaneous processing liquid and solid hydrocarbon material and installation to this end |
| CN103087769A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Delayed coking method |
| CN203419889U (en) * | 2013-07-17 | 2014-02-05 | 上海顶丰能源科技有限公司 | Processing system for recycling waste oil |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105316033A (en) * | 2015-12-03 | 2016-02-10 | 南京绿帝环保能源科技有限公司 | Thermal cracking device for waste oil and waste engine oil |
| CN105441122A (en) * | 2015-12-18 | 2016-03-30 | 云南新昊环保科技有限公司 | Waste mineral oil cycle flash evaporation catalytic cracking recovery process |
| CN105567309A (en) * | 2015-12-18 | 2016-05-11 | 云南新昊环保科技有限公司 | Waste mineral oil circulating flash-evaporation catalytic cracking recovery plant |
| CN105567309B (en) * | 2015-12-18 | 2018-01-09 | 云南新昊环保科技有限公司 | Waste mineral oil circulation flash distillation catalytic pyrolysis reclaimer |
| CN108102681A (en) * | 2017-12-06 | 2018-06-01 | 菏泽万清源环保科技有限公司 | Hazardous waste resource regeneration method |
| CN108048200A (en) * | 2018-01-30 | 2018-05-18 | 余永清 | Waste oil distills cracking and catalyzing system and production technology |
| CN108048200B (en) * | 2018-01-30 | 2023-01-20 | 重庆威博尔特机械制造有限公司 | Waste oil distillation cracking catalytic system and production process |
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| CN103509597B (en) | 2017-04-26 |
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