CN102908794B - Condensation diversion reduced pressure distiller in tank - Google Patents
Condensation diversion reduced pressure distiller in tank Download PDFInfo
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- CN102908794B CN102908794B CN201210322768.1A CN201210322768A CN102908794B CN 102908794 B CN102908794 B CN 102908794B CN 201210322768 A CN201210322768 A CN 201210322768A CN 102908794 B CN102908794 B CN 102908794B
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- distillate
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- 238000009833 condensation Methods 0.000 title claims abstract description 19
- 230000005494 condensation Effects 0.000 title claims abstract description 19
- 239000010913 used oil Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 231100000331 toxic Toxicity 0.000 claims abstract description 9
- 230000002588 toxic effect Effects 0.000 claims abstract description 9
- 210000005056 cell body Anatomy 0.000 claims description 32
- 230000008676 import Effects 0.000 claims description 9
- 239000012774 insulation material Substances 0.000 claims description 8
- 238000000034 method Methods 0.000 abstract description 10
- 230000008569 process Effects 0.000 abstract description 8
- 238000000197 pyrolysis Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 239000011368 organic material Substances 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 3
- 238000005292 vacuum distillation Methods 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 51
- 239000007789 gas Substances 0.000 description 33
- 239000007788 liquid Substances 0.000 description 20
- 238000001704 evaporation Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- 238000004821 distillation Methods 0.000 description 8
- 230000008020 evaporation Effects 0.000 description 8
- 230000006837 decompression Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
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- 238000004519 manufacturing process Methods 0.000 description 3
- 238000004806 packaging method and process Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000010687 lubricating oil Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000002207 thermal evaporation Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
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- 238000000746 purification Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to the vacuum distillation apparatus of organic materials, particularly condensation diversion reduced pressure distiller in a kind of tank.It comprises evaporator, radiator body, oil gas vent, exhaust of oil pipeline, condenser, distillate collecting tank, toxic emission pipeline, in described evaporator, the top of used oil is provided with guiding gutter, and this guiding gutter is communicated with described distillate gathering-device by water conservancy diversion pipeline.The present invention compared with prior art, by collect used oil when high-temperature heating evaporate because of meet cold and be condensed liquefy distillate, not only efficiently suppress distillate to be again back to and avoided excessive pyrolysis by the used oil that heats, can also reduce and a large amount of heat energy consumption, vacuum pressure reduction and flow process distance, also significantly can improve the operating efficiency of device.
Description
Technical field
The present invention relates to the vacuum distillation apparatus of organic materials, particularly condensation diversion reduced pressure distiller in a kind of tank.
Background technology
Decompression distillation is a kind of distillating method realizing reducing the energy-conservation of feed liquid boiling temperature and suppress the pyrolysis of distillation feed liquid by reducing air pressure, be widely used at present, but the degree of the energy saving of decompression distillation and the pyrolysis of suppression distillation feed liquid is the focus of current retort field technical staff.
A kind of decompression distillation device of the prior art, see accompanying drawing 1; In figure: evaporator 1, oil gas vent 6, exhaust of oil pipeline 10, vavuum pump 11, condenser 12, toxic emission pipeline 13, distillate 14, distillate collecting tank 15, used oil 18, evaporator support 19, radiator body 20.
Evaporator 1 is a horizontal tank container, is placed on evaporator support 19, its top is provided with oil gas vent 6, and within it middle and lower part is surrounded with radiator body 20 and is loaded with used oil 18, has insulation material at its outer packaging; Radiator body 20 is the disk-shaped tubes around being arranged on middle and lower part in evaporator 1, and the tank skin that the two ends of this disk-shaped tube passes through evaporator 1 respectively communicates with the external world; The import of exhaust of oil pipeline 10 is communicated with oil gas vent 6, the inlet communication of its outlet of this traversing pipe line condenser 12 and distillate collecting tank 15; Distillate collecting tank 15 be a vertical tank body container deposit on support, its upper end is provided with inserts the import of appropriate depth and outlet, and its internal gathering has distillate 14; The import of vavuum pump 11 is by the outlet of toxic emission pipeline 13 with distillate collecting tank 15; Also be equipped with feeding line and material inlet valve on the top of evaporator 1, be also equipped with discharge line and discharge valve in the bottom of distillate collecting tank 15.
Noted toward in evaporator 1 by material inlet valve and feeding line by used oil 18, its injection rate accounts for about 1/2nd of evaporator 1 volume.Utilize heat carrier at radiator body 20 Inner eycle, for the used oil 18 in evaporator 1 carries out heat release, used oil 18 temperature after being heated constantly rises, when reaching the evaporating temperature of used oil 18 under its vacuum pressure, Evaporation Phenomenon starts to occur, in used oil 18 at this moment, constantly have the high-temperature oil gas be vaporized to depart from used oil 18 liquid level constantly to rise, a part high-temperature oil gas by the first half tank skin of evaporator 1 because the temperature difference makes its cooling liquid, again be back to bottom by the used oil 18 that heats, another part can not be cooled liquefaction high-temperature oil gas, enter in exhaust of oil pipeline 10 via oil gas vent 6.
Enter the high-temperature oil gas in exhaust of oil pipeline 10, pass through condenser 12 to accept cool and enter in distillate collecting tank 15, the distillate 14 be liquefied through cooling is collected by distillate collecting tank 15, and the waste gas of the liquefaction that can not be cooled is discharged into the external world via toxic emission pipeline 13 and vavuum pump 11.
In the process of continual evaporation, in order to maintain the optimal liquid level of used oil 18 in evaporator 1, used oil feed-line is communicated with the material inlet valve of evaporator 1, via the feeding line of evaporator 1, appropriate used oil 18 is supplemented to the inside of evaporator 1.
The defect that the distiller of this structure exists is: a part of high-temperature oil gas by the first half tank skin of evaporator 1 because the temperature difference makes its cooling liquid, again be back to bottom by the used oil 18 that heats, again accept by thermal evaporation, not only reduce the energy saving of device thus, also exacerbate the degree of pyrolysis of distillation feed liquid, also reduce the working (machining) efficiency of device.
Chinese patent another molecular still disclosed, patent No. CN 101732881 A, its structure is that the acting part of distiller cylindrical shell is made up of the vertical chuck of circle, in chuck, there is heating agent conduction oil to be radiator body, condenser is provided with in jacket cylinder, be provided with between jacket cylinder inwall to condenser by lower flange, column and scrape lath composition rotating cage device, jacket cylinder top is provided with upper flange, material inlet, the rotating shaft be connected with rotating cage device, reductor and motor, vacuum port is respectively arranged with in jacket cylinder bottom, skewed slot, heavy oil exports, light oil feeder, light oil outlet etc., radial distance between the outside tube wall of this device condenser pipe and cylinder inboard wall is set to 3.6cm ~ 4.2cm.The internal diameter of cylindrical shell is arranged between 460mm ~ 580mm, and in cylindrical shell, working portion length is arranged between 1.3m ~ 1.8m.The shortcoming of this device is: because its compact accuracy is higher and miniaturized, be difficult to the cooked mode realizing long-time high production capacity, inadaptable processing higher boiling, thermal sensitivity requires higher, include more impurity and process the lower feed liquid of added value, otherwise: be only 3.6cm ~ 4.2cm because the radial distance between the outside tube wall of condenser pipe and cylinder inboard wall is arranged, be provided with between jacket cylinder inwall to condenser by lower flange, column and scrape lath composition rotating cage device, be very easy to make feed liquid drop splash on the outside tube wall of condenser pipe by cylinder inboard wall, form short circuit evaporation thus, the compact precise space of device is carried out dirt destroy because feed liquid includes solid formation that more Impurity Potential must produce within the shorter working time, device is entered in the longer time between overhauls(TBO) within the shorter working time.Due to the miniaturization of device, the working (machining) efficiency of device certainly will be caused low.Apparatus structure more complicated, easily cause the manufacturing cost of device and maintenance cost too high.
In sum: because the time between overhauls(TBO) of device is long, easily by shortening the production cycle of device, adding the factors such as working (machining) efficiency is low, finally can cause the economic benefit of the too high and very difficult embodiment feed liquid processing of processing charges.
Description below by quote by the description of this patent:
Feed liquid: the material referring to purification to be distilled, both: the raw material of distillate product.
Distillate: the liquid phase fraction that feed liquid obtains through cooling after heat vaporized evaporation is separated.
Flow process distance: in evaporation process, feed liquid liquid level is apart from the height distance can collecting distillate.
Summary of the invention
The object of the invention is to the deficiency overcoming background technology, and provide a kind of evaporator internal cause of collecting to meet cold reflux and the distillate that produces and condensation diversion reduced pressure distiller in the tank suppressing distillate to be back and forth heated.
The present invention solves its technical problem and adopts following technical scheme:
Condensation diversion reduced pressure distiller in a kind of tank, comprise evaporator, radiator body, oil gas vent, exhaust of oil pipeline, condenser, distillate collecting tank, toxic emission pipeline, in described evaporator, the top of used oil is provided with guiding gutter, and this guiding gutter is communicated with described distillate gathering-device by water conservancy diversion pipeline.
Adopt the present invention of technique scheme compared with prior art, by collect used oil when high-temperature heating evaporate because of meet cold and be condensed liquefy distillate, not only efficiently suppress distillate to be again back to and avoided excessive pyrolysis by the used oil that heats, can also reduce and a large amount of heat energy consumption, vacuum pressure reduction and flow process distance, also significantly can improve the operating efficiency of device.
Preferred version of the present invention is:
Described guiding gutter comprises cell body internal layer, cell body skin and cell body end plate, above-mentioned cell body internal layer, cell body skin and cell body end plate are interconnected to constitute airtight mezzanine space, be provided with the pod apertures run through between described cell body internal layer and cell body skin, this pod apertures is communicated with described water conservancy diversion pipeline.
Insulation material is filled with in described mezzanine space.
The uniform middle and upper part be arranged in evaporator of described guiding gutter, is provided with above this guiding gutter and evaporates tank connected first deflector.
The uniform middle and upper part be arranged in evaporator of described guiding gutter, is provided with the second deflector above between adjacent guide groove.
Be provided with liquefaction condenser between described second deflector, the import of this liquefaction condenser communicates with evaporator outside.
The outlet of described liquefaction condenser is arranged within evaporator.
The outlet of described liquefaction condenser is arranged at outside evaporator.
Described oil gas vent and water conservancy diversion pipeline outlet are communicated with same exhaust of oil pipeline respectively.
Described evaporator is the tank container of a horizontal type structure.
Accompanying drawing explanation
Fig. 1 is a kind of decompression distillation device of the prior art.
Fig. 2 is structural representation of the present invention.
Fig. 3 is evaporator inside top schematic diagram.
Fig. 4 is evaporator internal structure schematic diagram (removing the top view of liquefaction condenser).
Fig. 5 is the top view below evaporator internal diversion groove and guiding gutter support.
Fig. 6 is the top view of below evaporator internal diversion pipeline part.
Fig. 7 is guide trough structure schematic diagram.
Fig. 8 is the baffle structural representation of guiding gutter end.
Detailed description of the invention
Below in conjunction with drawings and Examples in detail the present invention is described in detail:
Organic materials is comprising waste lubricating oil, and following examples are extracted reclaimed lubricating base oil for waste lubricating oil decompression distillation and are described.
Condensation diversion reduced pressure distiller in a kind of tank, see accompanying drawing, in figure: evaporator 1, first deflector 2, second deflector 3, liquefaction condenser brackets 4, liquefaction condenser 5, liquefaction condenser inlet 51, liquefaction condenser first exports 52, liquefaction condenser second exports 53, first valve 54, second valve 55, oil gas vent 6, guiding gutter 7, pod apertures 71, cell body internal layer 72, cell body skin 73, mezzanine space 74, cell body end plate 75, deflector support 8, first guiding gutter support 9, exhaust of oil pipeline 10, vavuum pump 11, condenser 12, toxic emission pipeline 13, distillate 14, distillate collecting tank 15, water conservancy diversion pipeline 16, second guiding gutter support 17, used oil 18, evaporator support 19, radiator body 20.
In the present embodiment, evaporator 1 is the tank container of a horizontal type structure, be placed on evaporator support 19, the top of evaporator 1 is provided with oil gas vent 6, in evaporator 1, middle and lower part is surrounded with radiator body 20, and be loaded with used oil 18, evaporator 1 middle and upper part horizontal cross is connected with deflector support 8, below deflector support 8, distribution is connected with the first guiding gutter support 9, on tank skin between deflector support 8 and the first guiding gutter support 9, level is longitudinally connected with the first downward-sloping deflector 2, and the outer packaging of evaporator 1 has insulation material.Evaporator 1 is the tank container of horizontal type structure, the disengagement area of used oil 18 and water conservancy diversion can be collected area and realize maximizing.
In evaporator 1, the top of used oil 18 is provided with guiding gutter 7, and the bottom of guiding gutter 7 is communicated with distillate gathering-device by water conservancy diversion pipeline 16; Distillate gathering-device is distillate collecting tank 15.
The U-shaped structure of section of guiding gutter 7, guiding gutter 7 is made up of cell body internal layer 72, cell body outer 73 and cell body end plate 75, cell body internal layer 72, cell body outer 73 and cell body end plate 75 are interconnected to constitute airtight mezzanine space 74, two limits of cell body internal layer 72 are connected with two limits of cell body skin 73, and the two ends of cell body internal layer 72 and cell body skin 73 seal by cell body end plate 75; Be provided with the pod apertures 71 run through between cell body internal layer 72 and cell body skin 73, pod apertures 71 is communicated with water conservancy diversion pipeline 16.
In order to improve the heat-proof quality of guiding gutter 7 further, in mezzanine space 74, be filled with insulation material; Realize slowing down guiding gutter 7 shell by the degree of high-temperature oil gas condensation liquefaction by mezzanine space 74.
Oil gas vent 6 is placed in the top of evaporator 1 and is communicated with exhaust of oil pipeline 10, and the other end of exhaust of oil pipeline 10 is communicated with distillate collecting tank 15.
The uniform middle and upper part be arranged in evaporator 1 of guiding gutter 7, is provided with above the outermost guiding gutter in left and right two edges 7 and evaporates tank connected first deflector 2; By the first deflector 2, the distillate 14 on evaporator 1 tank skin above guiding gutter 7 is imported the inside of guiding gutter 7.
First deflector 2 is elongated metal plates, and metallic plate is that angle of inclination is welded with the tank skin of evaporator 1, and the side tilted upward is welded with the tank skin of evaporator 1, and the side under being tilted to extends to the top of the guiding gutter 7 that below is arranged.
The uniform middle and upper part be arranged in evaporator 1 of guiding gutter 7, the top between adjacent guide groove 7 is provided with the second deflector 3.Second deflector 3 is in angle steel shape structure, two limits of steel angle structure are above guiding gutter, by the angle of inclination in angle steel shape structure second deflector 3, not only the distillate that drops on the second deflector 3 can being imported the inside of guiding gutter 7, the inside of its lower distillate of the second deflector 3 by its angle of inclination importing guiding gutter 7 can also be attached to meeting cold liquefaction.
Be provided with liquefaction condenser 5 between second deflector 3, the import of liquefaction condenser 5 communicates with the outside of evaporator 1.The outlet of liquefaction condenser 5 is arranged within evaporator 1.The outlet of liquefaction condenser 5 is arranged at outside evaporator 1.The import of liquefaction condenser 5 communicates with evaporator 1 outside, by condenser 5 and the temperature difference of passing through between up high-temperature oil gas of liquefying, more high-temperature oil gas cooling fluid can be changed into distillate 14.
Liquefaction condenser 5 has three mouthfuls of tubular bodies be placed on the liquefaction condenser brackets 4 in evaporator 1 of spiraling formed by one, liquefaction condenser inlet 51 and liquefaction condenser second export 53 tank skins passing through evaporator 1 and communicate with the external world, liquefaction condenser first exports 52 and is arranged on and exports on the liquefaction condenser 5 in 53 evaporators 1 close to liquefaction condenser second, liquefaction condenser first export 52 and liquefaction condenser second export on 53 and be separately installed with the first valve 54 and the second valve 55.
Best heat exchange energy-saving effect is also realized in order to more collect distillate 14 in evaporator 1 while, the outlet of liquefaction condenser 5 is arranged within evaporator 1, by opening the first valve 54, closing the second valve 55 makes liquefaction condenser 5 meet the demands, the used oil feed-line that can continue to supplement used oil 18 in evaporator 1 is communicated with liquefaction condenser inlet 51, by the used oil 18 of normal temperature or lower temperature via liquefaction condenser inlet 51, pass through liquefaction condenser 5 and carry out heat exchange with high-temperature oil gas, high-temperature oil gas after heat exchange is liquefied as distillate 14, used oil 18 temperature after heat exchange raises, 52 are exported via liquefaction condenser first, first valve 54 enters in evaporator 1 by the used oil 18 of thermal evaporation.
The outlet of liquefaction condenser 5 is arranged at outside evaporator 1, by closing the first valve 54, opening the second valve 55 makes liquefaction condenser 5 meet the demands, can by the water under normal temperature via liquefaction condenser inlet 51, pass through liquefaction condenser 5 and carry out heat exchange with high-temperature oil gas, high-temperature oil gas after heat exchange is liquefied as distillate 14, and the hot water after heat exchange exports the 53, second valve 55 via liquefaction condenser second and is discharged into the external world.
Oil gas vent 1 is communicated with same exhaust of oil pipeline 10 respectively with the outlet of water conservancy diversion pipeline 16; The apparatus structure that can realize under increasing apparatus function, increasing device capbility efficiency is simplified.
On the uniform guiding gutter support be arranged in evaporator 1 of guiding gutter 7, the guiding gutter 7 of two edges part is placed on the first guiding gutter support 9, and the guiding gutter 7 of non-edge part is placed on the second guiding gutter support 17.
Radiator body 20 is the disk-shaped tubes around being arranged on middle and lower part in evaporator 1, and the tank skin that the two ends of disk-shaped tube passes through evaporator 1 respectively communicates with the external world.
The upper port of exhaust of oil pipeline 10 is communicated with oil gas vent 6, side ports and water conservancy diversion pipeline 16 outlet, and the inlet communication of condenser 12 and distillate collecting tank 15 is passed through in lower end.
Distillate collecting tank 15 be a vertical tank body container deposit on support, upper end is provided with inserts the import of appropriate depth and outlet, and internal gathering has distillate 14.
Vavuum pump 11 is the vacuum source of native system, and its import is by the outlet of toxic emission pipeline 13 with distillate collecting tank 15, and its outlet communicates with the external world.
The top of evaporator 1 is also equipped with feeding line and material inlet valve.
The bottom of distillate collecting tank 15 is also equipped with discharge line and discharge valve.
Also be filled with the cooling medium of flowing among liquefaction condenser 5, cooling medium can be water, can also be oil, also can be the used oil 18 etc. continuing to supplement in evaporator 1.
For keeping the mezzanine space 74 of sealing state, can to fill insulant material in it, insulation material can be air, heat-preservation cotton or for the vacuum under air.
Guiding gutter 7 is not limited to installation form arranged side by side cited in above-described embodiment, and it can also play by the installation form such as intersecting or other layout the effect that water conservancy diversion collects distillate 14.
Deflector both can be embodied by the form of the first deflector 2, can also be embodied, also can embody in other forms by the form of the second deflector 3, and it refers to the parts that the high temperature distillate 14 of the liquefaction that is condensed above it can be imported in guiding gutter 7.
Liquefaction condenser 5, deflector and guiding gutter 7 to be not limited in above-described embodiment cited form, can also play the effect that condensation and water conservancy diversion collect by the form such as to spiral or bending.
Radiator body 20 is not limited to form cited in above-described embodiment, can also realize its heat release function by modes such as electric heating or the direct heat releases of fuel combustion.
The description of the various embodiments described above is not all the restriction to the present invention program, any conceive according to the present invention done be only pro forma but not substantial equivalent transformation and all should be considered as technical scheme category of the present invention.
Noted toward in evaporator 1 by material inlet valve and feeding line by used oil 18, its injection rate accounts for about 1/2nd of evaporator 1 volume.
Utilizing heat carrier at radiator body 20 Inner eycle, for the used oil 18 in evaporator 1 carries out heat release, open vavuum pump 11, make distiller system realize vacuum decompression state, providing advantage for reducing used oil 18 boiling point.
Used oil 18 temperature after being heated constantly rises, and when reaching the evaporating temperature of used oil 18 under its vacuum pressure, Evaporation Phenomenon starts to occur, in used oil 18 now, constantly has the high-temperature oil gas be vaporized to depart from used oil 18 liquid level and constantly rises.
The gap passed through between guiding gutter 7 and guiding gutter 7 continues upwards to run by the high-temperature oil gas that disengaging used oil 18 liquid level constantly rises, part oil gas vent 6 of postponing enters in exhaust of oil pipeline 10, another part high-temperature oil gas is made it be cooled into liquid high temperature distillate 14 by the first half tank skin of evaporator 1 because of the temperature difference and is back in guiding gutter 7, under the effect of water conservancy diversion pipeline 16, the water conservancy diversion pipeline 16 of postponing of the liquid high temperature distillate 14 collected by diversed groove 7 enters in exhaust of oil pipeline 10.
Enter the high-temperature oil gas in exhaust of oil pipeline 10 and liquid high temperature distillate 14, condenser 12 will be passed through accept to cool and enter distillate collecting tank 15 inside, distillate 14 through cooling obtained is collected by distillate collecting tank 15, and the waste gas of the liquefaction that can not be cooled is discharged into the external world via toxic emission pipeline 13 and vavuum pump 11.
In the process of continual evaporation, in order to maintain the optimal liquid level of used oil 18 in evaporator 1, used oil feed-line is communicated with the material inlet valve of evaporator 1, via the feeding line of evaporator 1, appropriate used oil 18 is supplemented to the inside of evaporator 1.
Although the outer packaging of evaporator 1 has insulation material, but also there is the drawback of heat radiation in insulation material, in the inevitable temperature lower than high-temperature oil gas of first half tank wall temperature of evaporator 1 under evaporation operating mode of being heated, a fixed difference difference must be formed with high-temperature oil gas, under the effect of the temperature difference, must by a part of high-temperature oil gas condensation liquefaction.
By in evaporator 1 inside by the use in conjunction of guiding gutter 7 and water conservancy diversion pipeline 16, the high temperature distillate 14 produced because of cooling for reflux in evaporator 1 inside can be collected in time: not only efficiently suppress this distillate 14 to be again back to and avoided excessive pyrolysis in the used oil 18 that heats; Can also reduce need because this distillate 14 is back and forth heated heat energy consumption; By the high temperature distillate 14 obtained at evaporator 1 internal gathering, significantly can reduce the high-temperature oil gas volume producing this distillate 14, reduce the pressure reduction between evaporator 1 inside and vacuum source thus; In the structure of this device, the suitable for reading of guiding gutter 7 is the minimum altitude can collecting distillate 14, can shorten the flow process distance of high-temperature oil gas; And the operating efficiency of device can be improved further.
Claims (9)
1. condensation diversion reduced pressure distiller in a tank, comprise evaporator, radiator body, oil gas vent, exhaust of oil pipeline, condenser, distillate collecting tank, toxic emission pipeline, is characterized in that: in described evaporator, the top of used oil is provided with guiding gutter, and this guiding gutter is communicated with described distillate collecting tank by water conservancy diversion pipeline; Described guiding gutter comprises cell body internal layer, cell body skin and cell body end plate, above-mentioned cell body internal layer, cell body skin and cell body end plate are interconnected to constitute airtight mezzanine space, be provided with the pod apertures run through between described cell body internal layer and cell body skin, this pod apertures is communicated with described water conservancy diversion pipeline.
2. condensation diversion reduced pressure distiller in tank according to claim 1, is characterized in that: be filled with insulation material in described mezzanine space.
3. condensation diversion reduced pressure distiller in tank according to claim 1, is characterized in that: the uniform middle and upper part be arranged in evaporator of described guiding gutter, is provided with and evaporates tank connected first deflector above this guiding gutter.
4. condensation diversion reduced pressure distiller in tank according to claim 1, is characterized in that: the uniform middle and upper part be arranged in evaporator of described guiding gutter, is provided with the second deflector above between adjacent guide groove.
5. condensation diversion reduced pressure distiller in tank according to claim 4, it is characterized in that: be provided with liquefaction condenser between described second deflector, the import of this liquefaction condenser communicates with evaporator outside.
6. condensation diversion reduced pressure distiller in tank according to claim 5, is characterized in that: the outlet of described liquefaction condenser is arranged within evaporator.
7. condensation diversion reduced pressure distiller in tank according to claim 5, is characterized in that: the outlet of described liquefaction condenser is arranged at outside evaporator.
8. condensation diversion reduced pressure distiller in tank according to claim 1, is characterized in that: described oil gas vent and water conservancy diversion pipeline outlet are communicated with same exhaust of oil pipeline respectively.
9. condensation diversion reduced pressure distiller in tank according to claim 1, is characterized in that: described evaporator is the tank container of a horizontal type structure.
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| CN201210322768.1A CN102908794B (en) | 2012-09-04 | 2012-09-04 | Condensation diversion reduced pressure distiller in tank |
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| CN201210322768.1A CN102908794B (en) | 2012-09-04 | 2012-09-04 | Condensation diversion reduced pressure distiller in tank |
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| CN102908794B true CN102908794B (en) | 2015-07-29 |
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| US10711076B2 (en) * | 2018-11-29 | 2020-07-14 | GM Global Technology Operations LLC | Mobile vacuum distillation unit for transport of articles containing releasable volatile organic compounds |
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| CN1089298A (en) * | 1992-11-30 | 1994-07-13 | 布斯公司 | The deep processing technology of vacuum residuum in the crude oil refinery |
| CN102266677A (en) * | 2011-06-24 | 2011-12-07 | 刘元 | High vacuum distillation purification device |
| CN202724723U (en) * | 2012-09-04 | 2013-02-13 | 吴国存 | Condensation flow-guiding reduced pressure distillation device in tank |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3500331B2 (en) * | 1999-08-06 | 2004-02-23 | アクトファイブ株式会社 | Distillation regenerator |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1089298A (en) * | 1992-11-30 | 1994-07-13 | 布斯公司 | The deep processing technology of vacuum residuum in the crude oil refinery |
| CN102266677A (en) * | 2011-06-24 | 2011-12-07 | 刘元 | High vacuum distillation purification device |
| CN202724723U (en) * | 2012-09-04 | 2013-02-13 | 吴国存 | Condensation flow-guiding reduced pressure distillation device in tank |
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