CN101829434A - Convective heat exchange fractionation device - Google Patents
Convective heat exchange fractionation device Download PDFInfo
- Publication number
- CN101829434A CN101829434A CN201010199848A CN201010199848A CN101829434A CN 101829434 A CN101829434 A CN 101829434A CN 201010199848 A CN201010199848 A CN 201010199848A CN 201010199848 A CN201010199848 A CN 201010199848A CN 101829434 A CN101829434 A CN 101829434A
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- transferring medium
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- 238000005194 fractionation Methods 0.000 title abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 56
- 239000007791 liquid phase Substances 0.000 claims abstract description 14
- 238000012856 packing Methods 0.000 claims description 12
- 238000004891 communication Methods 0.000 claims description 7
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000004821 distillation Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract 2
- 239000010705 motor oil Substances 0.000 abstract 2
- 239000002699 waste material Substances 0.000 abstract 2
- 239000003921 oil Substances 0.000 abstract 1
- 239000010913 used oil Substances 0.000 description 15
- 239000007789 gas Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 238000000746 purification Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 6
- 230000011218 segmentation Effects 0.000 description 6
- 238000001816 cooling Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the oil distillation technology, in particular to a convection heat exchange fractionation device, which comprises an evaporating pot, an oil-gas drainage pipeline, a gas-liquid separator and a component gathering tank. The gas-liquid separator is set on the oil-gas drainage pipeline; a convection heat exchanger is sleeved on the oil-gas drainage pipeline between the gas-liquid separator and the evaporating pot; a heat exchange medium inlet of the convection heat exchanger is communicated with a material tank through a metering conveyor, and a heat exchange medium outlet of the convection heat exchanger is communicated with the inside of the evaporating tank through a heat exchange medium output pipeline; and the lower port of the gas-liquid separator is communicated with the component gathering tank through a liquid-phase condenser. In the invention, as the input port of the convection heat exchanger is communicated with the material tank through the metering conveyor, and the output port of the convection heat exchanger is communicated with the inside of the evaporating pot through the heat exchange medium output pipeline, the flowing directions of the waste engine oil as heat exchange medium and the high-temperature oil-gas are in convection trend; moreover, the waste engine oil is pre-heated by fractionation temperature difference The invention has the advantages of high efficiency, energy saving, simple device structure and stable fractionation performance.
Description
Technical field:
The present invention relates to the oil plant distillation technique, particularly a kind of heat convection fractionating device.
Background technology:
Oil plant is comprising used oil, and it is made up of many components, and component is light more, and its boiling range temperature is low more.
Be example with above-mentioned used oil below, distill purification processes.
The evaporation of tradition used oil is purified and is generally adopted following three kinds of methods:
1. segmentation heat, the segmentation method of purification: utilize under different boiling range temperature, obtain the principle of different fractions, to its distillation purification processes of heating, the technology of heating is from low to high, by under different boiling range temperature, obtain different cuts respectively and carry out fractionation.2. vertical fractionating column method of purification: the used oil in evaporimeter provides the boiling range temperature that can make heavy component evaporation in it, light component, middle component, heavy component in the used oil are evaporated simultaneously, carry out fractionation by the principle that the different fractionation height and the height of lifting of light more its oil gas of component of oil plant of vertical fractionating column are high more.3. continuous multi-stage segmentation method of purification: a plurality of evaporimeters of arranged in series and cooling gathering system, heating-up temperature,, is obtained different cuts respectively and is carried out fractionation by under different boiling range temperature by high by low.
The defective that said method exists is:
1. segmentation heat, the segmentation method of purification: efficient is too low, the tail oil in later stage is because of the evaporation liquid level descends, and causes its oil gas height of lifting constantly to raise, and finally causes at high temperature the part heavy component being cracked into light component and can not effectively separating it.
2. vertical fractionating column method of purification: fractionating column internal structure complexity, very strict to the requirement for height of equipment.
3. continuous multi-stage segmentation method of purification: equipment investment and floor space are too big.
Summary of the invention:
The objective of the invention is to overcome the deficiency of background technology and provide a kind of simple in structure, utilize used oil to do heat transferring medium, can utilize the fractionation temperature difference for the preheating of raw material used oil, can effectively separate the heat convection fractionating device that mixes each component in the high-temperature oil gas.
The technical scheme that the present invention solves its technical problem employing is:
A kind of heat convection fractionating device, comprise evaporator, the exhaust of oil pipeline that is communicated with evaporator top, gas-liquid separator, the component collecting tank, described exhaust of oil pipeline is provided with gas-liquid separator, be set with convection recuperator on the exhaust of oil pipeline between this gas-liquid separator and the evaporator, the heat transferring medium inlet of this convection recuperator is communicated with head tank by metering and conveying device, the heat transferring medium outlet of this convection recuperator is by heat transferring medium export pipeline and evaporator internal communication, and the lower port of gas-liquid separator is communicated with the component collecting tank by the liquid phase condensate device.
The present invention of employing technique scheme compared with prior art, on the exhaust of oil pipeline, be set with convection recuperator, the medium input port of convection recuperator is communicated with head tank by metering and conveying device, the medium output port of convection recuperator is by heat transferring medium export pipeline and evaporator internal communication, makes the used oil of doing heat transferring medium and the flow direction of high-temperature oil gas be the convection current tendency; Can utilize the fractionation temperature difference to be the preheating of raw material used oil, with this realize energy-efficient, apparatus structure is simple, fractionation performance is stable.
As a preferred embodiment of the present invention, the gas-liquid separator that is provided with at interval on the described exhaust of oil pipeline is followed successively by the heavy ends gas-liquid separator, middle component gas-liquid separator and light component gas-liquid separator, be set with first convection recuperator on the exhaust of oil pipeline between described heavy ends gas-liquid separator and the middle component gas-liquid separator, the lower port of component gas-liquid separator is communicated with middle component collecting tank by the first liquid phase condensate device in described, be set with second convection recuperator on the exhaust of oil pipeline between described heavy ends gas-liquid separator and the evaporator, the lower port of this heavy component gas-liquid separator is communicated with the heavy component collecting tank by the second liquid phase condensate device; The heat transferring medium inlet of described first convection recuperator is communicated with head tank by metering and conveying device, the heat transferring medium outlet of this first convection recuperator is communicated with the heat transferring medium inlet of second convection recuperator by the heat transferring medium connecting line, and the heat transferring medium outlet of this second convection recuperator is by heat transferring medium export pipeline and evaporator internal communication.
As a preferred embodiment of the present invention, described convection recuperator comprises the heat exchanger overcoat, the two ends of this heat exchanger overcoat are respectively equipped with ring flange and packing seal assembly, the outer wall of this ring flange and exhaust of oil pipeline is affixed, this packing seal assembly is sleeved on the described exhaust of oil pipeline, and this heat exchanger overcoat is respectively equipped with thermal medium inlet and thermal medium outlet near the two ends of described packing seal assembly and ring flange.
As a preferred embodiment of the present invention, described metering and conveying device is the positive displacement delivery pump of adjustable speed.
As a preferred embodiment of the present invention, described metering and conveying device is the valve that can regulate aperture.
Description of drawings:
Fig. 1 is a structural representation of the present invention.
Fig. 2 is the structural representation of convection recuperator among the present invention.
The specific embodiment:
Below in conjunction with drawings and Examples in detail the present invention is described in detail:
A kind of heat convection fractionating device is referring to accompanying drawing 1, accompanying drawing 2; Among the figure: evaporator 1, exhaust of oil pipeline 2, heat transferring medium export pipeline 3, second convection recuperator 4, heat transferring medium connecting line 5, heavy component gas-liquid separator 6, first convection recuperator 7, metering and conveying device 8, heat transferring medium intake pipeline 9, head tank 10, middle component gas-liquid separator 11, gas-liquid condenser 12, light component gas-liquid separator 13, oiliness toxic emission pipeline 14, light component feed-line 15, light component collecting tank 16, middle component collecting tank 17, the first liquid phase condensate device 18, heavy component collecting tank 19, the second liquid phase condensate devices 20, heat exchanging medium passage 21, heat exchanger overcoat 22, packing seal assembly 23, heat transferring medium inlet 24, ring flange 25, bolt 26, heat transferring medium outlet 27.
In the present embodiment, evaporator 1 is sealed bucket body structure, the exhaust of oil pipeline 2 that is communicated with evaporator 1 top, exhaust of oil pipeline 2 is provided with gas-liquid separator, be set with convection recuperator on the exhaust of oil pipeline 2 between gas-liquid separator and the evaporator 1, the heat transferring medium inlet 24 of convection recuperator is communicated with head tank 10 by metering and conveying device 8, the heat transferring medium outlet 27 of convection recuperator is by heat transferring medium export pipeline 3 and evaporator 1 internal communication, and the lower port of gas-liquid separator is communicated with the component collecting tank by the liquid phase condensate device.
A kind of preferred structure as present embodiment, the gas-liquid separator that is provided with at interval on the exhaust of oil pipeline 2 is followed successively by heavy ends gas-liquid separator 6, middle component gas-liquid separator 11 and light component gas-liquid separator 13, be set with first convection recuperator 7 on the exhaust of oil pipeline 2 between heavy ends gas-liquid separator 6 and the middle component gas-liquid separator 11, the lower port of middle component gas-liquid separator 11 is communicated with middle component collecting tank 17 by the first liquid phase condensate device 18, be set with second convection recuperator 4 on the exhaust of oil pipeline 2 between heavy ends gas-liquid separator 6 and the evaporator 1, the lower port of heavy component gas-liquid separator 6 is communicated with heavy component collecting tank 19 by the second liquid phase condensate device 20; The heat transferring medium inlet 24 of first convection recuperator 7 is communicated with head tank 10 by metering and conveying device 8, the heat transferring medium outlet 27 of first convection recuperator 7 is communicated with the heat transferring medium inlet 24 of second convection recuperator 4 by heat transferring medium connecting line 5, and the heat transferring medium outlet 27 of second convection recuperator 4 is by heat transferring medium export pipeline 3 and evaporator 1 internal communication.
Heavy ends gas-liquid separator 6, middle component gas-liquid separator 11 and light component gas-liquid separator 13 are three-port structure.
The two ends of the heat exchanger overcoat 22 in first convection recuperator 7 are respectively equipped with ring flange 25 and packing seal assembly 23, ring flange or the arc installed on ring flange 25 and exhaust of oil pipeline 2 outer walls are affixed, packing seal assembly 23 is sleeved on the exhaust of oil pipeline 2, and heat exchanger overcoat 22 is respectively equipped with heat transferring medium inlet 24 and heat transferring medium outlet 27 near the two ends of packing seal assembly 23 and ring flange 25.
The structure of second convection recuperator 4 is identical with the structure of first convection recuperator 7.
As a kind of preferred structure of the present invention, metering and conveying device 8 can be the positive displacement delivery pump of adjustable speed, also can be the valve that can regulate aperture.
Operation principle:
The used oil that accounts for total measurement (volume) 1/2nd is equipped with in evaporator 1 inside, under the effect of other thermal source, its interior used oil is constantly heated up, during mixed composition boiling range temperature within heat source temperature reaches used oil, outwards discharged by the mixed composition oil gas of the steam raising exhaust of oil pipeline 2 of postponing, open metering and conveying device 8 to first convection recuperator 7 this moment, the an amount of used oil raw material of carrying is done heat transferring medium in second convection recuperator 4, high temperature mixed oil and gas in heat transferring medium in the heat exchanger overcoat 22 and the exhaust of oil pipeline 2 is the convection current tendency, continues to be subjected to thermal evaporation through the used oil behind the highly effective gathering waste heat in heat transferring medium export pipeline 3 enters evaporator 1; The heavy component that is sleeved in the high temperature mixed oil and gas in the exhaust of oil pipeline 2 in second convection recuperator 4 can preferentially be liquefied, the lower port of heavy component gas-liquid separator 6 of postponing enters in the second liquid phase condensate device 20 accepts cooling, collected through cooled heavy component by heavy component collecting tank 19, the mixed oil and gas that does not coagulate is entered in the exhaust of oil pipeline 2 that is sleeved in first convection recuperator 7 by a side outlet of heavy component gas-liquid separator 6 and continues to accept heat convection, middle component after heat exchange in the mixed oil and gas is liquefied again, the lower port of component gas-liquid separator 11 of postponing enters in the first liquid phase condensate device 18 accepts cooling, component collecting tank 17 is collected in the component quilt in cooled, a side outlet of component gas-liquid separator 11 enters in the gas-liquid condenser 12 that is sleeved on the exhaust of oil pipeline 2 and accepts degree of depth condensing heat-exchange in the light component oil gas warp that does not coagulate, the cooling that also can be liquefied of light component behind degree of depth condensing heat-exchange in the mixed oil and gas, the lower port of light component gas-liquid separator 13 of postponing is collected by light component collecting tank 16 via light component feed-line 15, and the oiliness waste gas that does not coagulate is discharged into the external world via oiliness toxic emission pipeline 14.
The two ends of heat exchanger overcoat 22 constitute heat exchanging medium passage 21 by the space between ring flange 25 and packing seal assembly 23 and the exhaust of oil pipeline 2, ring flange 25 and packing seal assembly 23 can be realized the dismounting disintegration easily, not only can clear up at any time because of the formed heat exchange obstacle of used oil high-temperature coking, also can pass through the slidably property of filler assembly 23 on exhaust of oil pipeline 2 outer walls, will discharge absorption from the thermal stress of each side.
Adjusting can be realized by the conveying capacity that changes metering conveying pump 8, adjusting can be realized fractionating degree by the initial temperature that changes heat transferring medium to repairing speed.
The invention is not restricted to the structure of one or two cited in the foregoing description convection recuperator; also can adopt more convection recuperator to carry out the heat exchange fractionation according to actual needs; as long as after having adopted convection recuperator; still need to cool off again, all be considered as within protection scope of the present invention by condenser.
Claims (5)
1. heat convection fractionating device, comprise evaporator, the exhaust of oil pipeline that is communicated with evaporator top, gas-liquid separator, the component collecting tank, it is characterized in that: described exhaust of oil pipeline is provided with gas-liquid separator, be set with convection recuperator on the exhaust of oil pipeline between this gas-liquid separator and the evaporator, the heat transferring medium inlet of this convection recuperator is communicated with head tank by metering and conveying device, the heat transferring medium outlet of this convection recuperator is by heat transferring medium export pipeline and evaporator internal communication, and the lower port of gas-liquid separator is communicated with the component collecting tank by the liquid phase condensate device.
2. heat convection fractionating device according to claim 1, it is characterized in that: the gas-liquid separator that is provided with at interval on the described exhaust of oil pipeline is followed successively by the heavy ends gas-liquid separator, middle component gas-liquid separator and light component gas-liquid separator, be set with first convection recuperator on the exhaust of oil pipeline between described heavy ends gas-liquid separator and the middle component gas-liquid separator, the lower port of component gas-liquid separator is communicated with middle component collecting tank by the first liquid phase condensate device in described, be set with second convection recuperator on the exhaust of oil pipeline between described heavy ends gas-liquid separator and the evaporator, the lower port of this heavy component gas-liquid separator is communicated with the heavy component collecting tank by the second liquid phase condensate device; The heat transferring medium inlet of described first convection recuperator is communicated with head tank by metering and conveying device, the heat transferring medium outlet of this first convection recuperator is communicated with the heat transferring medium inlet of second convection recuperator by the heat transferring medium connecting line, and the heat transferring medium outlet of this second convection recuperator is by heat transferring medium export pipeline and evaporator internal communication.
3. heat convection fractionating device according to claim 1, it is characterized in that: described convection recuperator comprises the heat exchanger overcoat, the two ends of this heat exchanger overcoat are respectively equipped with ring flange and packing seal assembly, the outer wall of this ring flange and exhaust of oil pipeline is affixed, this packing seal assembly is sleeved on the described exhaust of oil pipeline, and this heat exchanger overcoat is respectively equipped with heat transferring medium inlet and heat transferring medium outlet near the two ends of described packing seal assembly and ring flange.
4. heat convection fractionating device according to claim 1 is characterized in that: described metering and conveying device is the positive displacement delivery pump of adjustable speed.
5. heat convection fractionating device according to claim 1 is characterized in that: described metering and conveying device is the valve that can regulate aperture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101998483A CN101829434B (en) | 2010-06-11 | 2010-06-11 | Convective heat exchange fractionation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101998483A CN101829434B (en) | 2010-06-11 | 2010-06-11 | Convective heat exchange fractionation device |
Publications (2)
| Publication Number | Publication Date |
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| CN101829434A true CN101829434A (en) | 2010-09-15 |
| CN101829434B CN101829434B (en) | 2012-07-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2010101998483A Expired - Fee Related CN101829434B (en) | 2010-06-11 | 2010-06-11 | Convective heat exchange fractionation device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102225239A (en) * | 2011-05-20 | 2011-10-26 | 吴国存 | Multilevel heat-exchange distilling device for dreggy organic materials |
| CN102847333A (en) * | 2012-09-04 | 2013-01-02 | 吴国存 | Reduced-pressure short path molecule distiller |
| CN102872608A (en) * | 2012-09-04 | 2013-01-16 | 吴国存 | High-position material supplying short-distance reduced pressure distiller |
| CN103482715A (en) * | 2013-09-16 | 2014-01-01 | 惠州Tcl环境科技有限公司 | High-concentration organic waste water evaporating and concentration processing method |
| CN112710169A (en) * | 2020-12-07 | 2021-04-27 | 重庆环纽信息科技有限公司 | Waste heat utilization device of waste oil regeneration rectification catalytic system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04120197A (en) * | 1990-09-11 | 1992-04-21 | Toyo Seisakusho:Kk | Purifying device of waste oil |
| CN2934235Y (en) * | 2006-07-07 | 2007-08-15 | 吴国存 | Device for regeneration of lubrication oil fuel by oiliness waste slag waste oil |
| CN201171923Y (en) * | 2008-04-14 | 2008-12-31 | 吴国存 | Oil material cracking evaporating waste gas treatment device |
| CN201692679U (en) * | 2010-06-11 | 2011-01-05 | 吴国存 | Convection heat exchange fractionation device |
-
2010
- 2010-06-11 CN CN2010101998483A patent/CN101829434B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04120197A (en) * | 1990-09-11 | 1992-04-21 | Toyo Seisakusho:Kk | Purifying device of waste oil |
| CN2934235Y (en) * | 2006-07-07 | 2007-08-15 | 吴国存 | Device for regeneration of lubrication oil fuel by oiliness waste slag waste oil |
| CN201171923Y (en) * | 2008-04-14 | 2008-12-31 | 吴国存 | Oil material cracking evaporating waste gas treatment device |
| CN201692679U (en) * | 2010-06-11 | 2011-01-05 | 吴国存 | Convection heat exchange fractionation device |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102225239A (en) * | 2011-05-20 | 2011-10-26 | 吴国存 | Multilevel heat-exchange distilling device for dreggy organic materials |
| CN102847333A (en) * | 2012-09-04 | 2013-01-02 | 吴国存 | Reduced-pressure short path molecule distiller |
| CN102872608A (en) * | 2012-09-04 | 2013-01-16 | 吴国存 | High-position material supplying short-distance reduced pressure distiller |
| CN102872608B (en) * | 2012-09-04 | 2015-04-08 | 唐山山岛石油化学有限公司 | High-position material supplying short-distance reduced pressure distiller |
| CN102847333B (en) * | 2012-09-04 | 2015-09-09 | 唐山山岛石油化学有限公司 | Decompression short-range molecular distillation device |
| CN103482715A (en) * | 2013-09-16 | 2014-01-01 | 惠州Tcl环境科技有限公司 | High-concentration organic waste water evaporating and concentration processing method |
| CN103482715B (en) * | 2013-09-16 | 2016-03-16 | 惠州Tcl环境科技有限公司 | A kind of high concentrated organic wastewater evaporation concentration treatment process |
| CN112710169A (en) * | 2020-12-07 | 2021-04-27 | 重庆环纽信息科技有限公司 | Waste heat utilization device of waste oil regeneration rectification catalytic system |
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| Publication number | Publication date |
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| CN101829434B (en) | 2012-07-18 |
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