CN103756717B - A kind of waste mineral oil distillation plant - Google Patents
A kind of waste mineral oil distillation plant Download PDFInfo
- Publication number
- CN103756717B CN103756717B CN201410019277.9A CN201410019277A CN103756717B CN 103756717 B CN103756717 B CN 103756717B CN 201410019277 A CN201410019277 A CN 201410019277A CN 103756717 B CN103756717 B CN 103756717B
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- Prior art keywords
- reactor
- nitrogen
- mineral oil
- waste mineral
- oil
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- 238000004821 distillation Methods 0.000 title claims abstract description 49
- 239000002699 waste material Substances 0.000 title claims abstract description 23
- 239000002480 mineral oil Substances 0.000 title claims abstract description 22
- 235000010446 mineral oil Nutrition 0.000 title claims abstract description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 86
- 239000003921 oil Substances 0.000 claims abstract description 45
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 42
- 238000010438 heat treatment Methods 0.000 claims abstract description 21
- 238000002347 injection Methods 0.000 claims abstract description 19
- 239000007924 injection Substances 0.000 claims abstract description 19
- 238000011049 filling Methods 0.000 claims abstract description 15
- 239000012530 fluid Substances 0.000 claims description 25
- 239000007789 gas Substances 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 23
- 239000013589 supplement Substances 0.000 claims description 8
- 230000006698 induction Effects 0.000 claims description 3
- 238000003756 stirring Methods 0.000 abstract description 5
- 230000009471 action Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 description 7
- 238000000034 method Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000000889 atomisation Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 238000010992 reflux Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000002199 base oil Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention proposes a kind of waste mineral oil distillation plant, comprise: reactor, distillation tower, outside pipeline road, injection tubing, condenser, receive oil tank, filling tank, heating unit, Nitrogen plant group, vacuum pump set, described distillation tower to be located at above described reactor and to be connected described condenser, described receipts oil tank one end is connected with described condenser by pipeline, the other end is connected with described vacuum pump set by pipeline, described outside pipeline road one end is connected with described filling tank, the other end connects with the injection tubing being positioned at described reactor inside, described heating unit is supplied to described distillation tower and described outside pipeline road heat energy, nitrogen is delivered to described reactor inside by the nitrogen blanketing valve road extending into described reactor inside by described Nitrogen plant group, by the pulling function of described vacuum pump set and the promotion stirring action of described Nitrogen plant group, output and the yield of finished product can be improved, reduce costs.
Description
Technical field
The present invention relates to oil product and refine field, refer to a kind of waste mineral oil distillation plant especially.
Background technology
Because mineral wet goods all belongs to Nonrenewable resources, and, in the process used, the waste of oil product, global energy dilemma etc., the regeneration carrying out waste mineral oil has been refined into more and more important, in traditional waste mineral oil distillation refining equipment, due to the restriction of device structure, such as heating installation temperature control is forbidden, cause in extractive process, Discrete control out of true, and, because oil gas is in moving process, many resistances can be subject to and temperature reduces, then reflux, for preventing this phenomenon, traditional way adds some lagging materials at outer walls such as distillation towers, but the effect done like this is unsatisfactory, in traditional reactor, together with the fluid seethed with excitement in oil gas and the bottom of rising usually mixes and stirs, and, bottom fluid is owing to being in reactor inside, also be inconvenient to stir, cause by heat trnasfer uneven, gas-liquid is not easily separated, the oil gas produced is difficult to transfer, directly cause the yield of product very low, cost raises etc., therefore, market needs a kind of more advanced waste mineral oil distillation plant.
Summary of the invention
The present invention proposes a kind of waste mineral oil distillation plant, solve above-mentioned in the problem mentioned.
Technical scheme of the present invention is achieved in that a kind of waste mineral oil distillation plant, comprise: reactor, distillation tower, outside pipeline road, injection tubing, condenser, receive oil tank, filling tank, heating unit, Nitrogen plant group, vacuum pump set, described distillation tower to be located at above described reactor and to be connected described condenser, described receipts oil tank one end is connected with described condenser by pipeline, the other end is connected with described vacuum pump set by pipeline, described outside pipeline road one end is connected with described filling tank, the other end connects with the injection tubing being positioned at described reactor inside, described heating unit is supplied to described distillation tower and described outside pipeline road heat energy, nitrogen is delivered to described reactor inside by the nitrogen blanketing valve road extending into described reactor inside by described Nitrogen plant group.
Further, described heating unit is the well heater frequently that shakes, comprising shake heater coil, fluid frequently of shake frequently heating unit and the oil gas that is connected electrically to shake heater coil frequently, described oil gas shakes frequently, and heater coil wraps is in described distillation tower periphery, and described fluid shakes frequency heater coil wraps at the described outside pipeline road outer wall of part.
Further, described in the frequently well heater that shakes be induction heating, frequency is 7-20kHz, and heated constant temperature scope is 160-500 DEG C, and temperature control adopts PID to regulate.
Further, the opening in described nitrogen blanketing valve road is located at apart from 200-300mm place at the bottom of the still of described reactor, and the opening end in described nitrogen blanketing valve road is provided with and fills nitrogen spiral nozzle.
Further, the pipe number of described nitrogen blanketing valve road in described reactor is 2, and caliber is 1/4-1 inch, and filling nitrogen flow is 5-20m
3/ h.
Further, described injection tubing is detachably provided with several spiral nozzles for oil spout, described spiral nozzle is conical hollow.
Further, the taper base angle of described spiral nozzle is 60 °, and described spiral nozzle fluid area is 1:1.3 ~ 1:1.5 with the ratio of described injection tubing open area.
Further, described reactor is inner, be positioned at below described injection tubing and be provided with gas-liquid phase-splitting net, described gas-liquid phase-splitting net is apart from the still top 600-1000mm of described reactor, described reactor is divided into upper and lower two spaces by described gas-liquid phase-splitting net, wherein, the volumetric ratio of upper space and described reactor is 1:5 ~ 1:3.
Further, described gas-liquid phase-splitting is on the net just provided with oil-air pressure to the part of distillation tower and supplements mouth, the hole of described oil-air pressure supplements mouth to be diameter be 400-600mm.
Further, also vacuum buffer tank is provided with between described receipts oil tank and described vacuum pump set.
Other structures are with reference to prior art.
The present invention has following beneficial effect:
1. matched with by described vacuum pump set by described Nitrogen plant group, described Nitrogen plant group can play a role in promoting to oil gas, and described vacuum pump set can play traction action to oil gas, push-and-pull action is just as four-wheel drive, thus oil gas is obtained resistance that enough energy break through on-way resistance and filler, overcome the refluence in oil-gas migration process, eliminate the Repeat-heating loss of flowing backwards and producing, arrive condenser and be cooled to base oil, improve the output of oil product.
2. by heating described distillation tower and described outside pipeline road at described heating unit, thus when oil gas arrives distillation tower from reactor, heat temperature raising can be carried out to oil gas, prevent oil gas from lowering the temperature and reflux, and then boost productivity and percent of pass, and, adopt for described in shake frequently well heater, use safety, simple operation, and temperature controls precisely, and practicality is extremely strong
3. in the present invention, also creationary spiral nozzle is used for oil atomization field, thus improves the effect of atomization greatly, and by pipe diameter size, the control of ratio, obtains best atomizing effect.
4. by described gas-liquid phase-splitting net, described reactor is divided into upper and lower two spaces, top is flash boiling spray vaporizing chamber, bottom is that fluid stores, teeter column, fluid is vaporized on top, the fluid having little time to gasify declines and encounters described gas-liquid phase-splitting net and decline and be obstructed, risen by the nitrogen band that rises along gas-liquid phase-splitting mesh, continue gasification, the fluid not arriving cut point temperature flows to bottom along gas-liquid phase-splitting mesh.Bottom is intercepted by described gas-liquid phase-splitting net by the fluid of nitrogen gas stirring, prevents from rushing tower.Secondly, the flash boiling spray vaporizer in the online portion of gas-liquid phase-splitting, provides and how to change regardless of fluid amount in distillation reactor, have the flash boiling spray gasification space that stable.Again, the vacuum tightness that described oil-air pressure supplements mouth place is relatively high, and the oil gas that bottom fluid has little time to gasify is stirred promotion by nitrogen, to go directly described distillation tower along oil-air pressure balance port.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation of a kind of waste mineral oil distillation plant of the present invention embodiment;
Fig. 2 is nitrogen blanketing valve road and the structural representation filling nitrogen spiral nozzle;
Fig. 3 is the structural representation of injection tubing and spiral nozzle;
Fig. 4 is the structural representation (looking down above reactor) of gas-liquid phase-splitting net.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
As Fig. 1, Fig. 2, Fig. 3, shown in Fig. 4, a kind of waste mineral oil distillation plant, comprise: reactor 1, distillation tower 2, outside pipeline road 3, injection tubing 4, condenser 5, receive oil tank 6, filling tank 7, heating unit 8, Nitrogen plant group 9, vacuum pump set 10, distillation tower 2 to be located at above reactor 1 and to be connected condenser 5, receive oil tank 6 one end to be connected with condenser 5 by pipeline, the other end is connected with vacuum pump set 10 by pipeline, outside pipeline road 3 one end is connected with filling tank 7, the other end connects with the injection tubing 4 being positioned at reactor 1 inside, heating unit 8 is supplied to distillation tower 2 and outside pipeline road 4 heat energy, nitrogen is delivered to reactor 1 inside by the nitrogen blanketing valve road 91 extending into reactor 1 inside by Nitrogen plant group 9.
Further, heating unit 8 is the well heater frequently that shakes, comprising shake heater coil 81, fluid frequently of shake frequently heating unit and the oil gas that is connected electrically to shake heater coil 82 frequently, the oil gas frequently heater coil 81 that shakes is wrapped in distillation tower 2 periphery, and the fluid heater coil 82 frequently that shakes is wrapped in portion of external pipeline road 4 outer wall.
Further, the well heater frequently that shakes is induction heating, and frequency is 7-20kHz, and heated constant temperature scope is 160-500 DEG C, and temperature control adopts PID to regulate.
Further, the opening in nitrogen blanketing valve road 91 is located at apart from 200-300mm place at the bottom of the still of reactor 1, and the opening end in nitrogen blanketing valve road 91 is provided with and fills nitrogen spiral nozzle 92.
Further, nitrogen blanketing valve road 91 pipe number is in a kettle. 2, and caliber is 1/4-1 inch, and filling nitrogen flow is 5-20m
3/ h.
Further, injection tubing 4 is detachably provided with several spiral nozzles 41 for oil spout, spiral nozzle 41 is in conical hollow.
Further, the taper base angle of spiral nozzle 41 is 60 °, and spiral nozzle 41 fluid area is 1:1.3 ~ 1:1.5 with the ratio of injection tubing 4 open area.
Further, reactor 1 is inner, is positioned at below injection tubing 4 and is provided with gas-liquid phase-splitting net 11, gas-liquid phase-splitting net 11 is apart from the still top 600-1000mm of reactor 1, reactor 1 is divided into upper and lower two spaces by gas-liquid phase-splitting net 11, and wherein, the volumetric ratio of upper space and reactor 1 is 1:5 ~ 1:3.
Further, gas-liquid phase-splitting net 11 is just provided with oil-air pressure to the part of distillation tower and supplements mouth 12, oil-air pressure supplement mouth 12 for diameter be the hole of 400-600mm.
Further, receive between oil tank 6 and vacuum pump set 10 and be also provided with vacuum buffer tank 101.
Other are with reference to prior art.
During use, waste mineral oil in filling tank 7 is through outside pipeline road 3, injection tubing 4, and enter into reactor 1 by spiral nozzle 41, wherein, in outside pipeline road 3, default temperature is heated to by the fluid of the frequently well heater of the shaking heater coil 82 frequently that shakes, then flash atomization in reactor 1, wherein, due to the structure of spiral nozzle 41 and fluid area and open area ratio, can fluid be made to greatest extent to spread, promote atomizing effect, after atomization, oil gas rises, enter distillation tower 2, due to the resistance etc. along journey, the temperature of oil gas can be caused to reduce, now heated by the oil gas frequently heater coil 81 pairs of distillation towers 2 that shake, then oil gas is transferred heat to, thus prevent oil gas from refluxing because resistance causes temperature reduction or be converted into lower of fluid, in reactor 1, the oil gas that flash distillation is formed is in the upper space of gas-liquid phase-splitting net 11, not easily sink to having the fluid of bottom to contact through this gas-liquid phase-splitting net 11, and, also can prevent the too high boiling of the oil liquid temperature of bottom from filling tower, and supplement mouth at oil-air pressure, vacuum tightness relatively large (distillation tower 2 that distance vacuum tightness is the highest is nearest) therefore, the fluid much having little time to vaporize directly enters into distillation tower under the drive of stream of nitrogen gas, improve percent of pass, in the bottom of reactor 1, because nitrogen is brought into by nitrogen blanketing valve road 91, and disperse under the effect of filling nitrogen spiral nozzle 92, the fluid of bottom is played to the effect of stirring, add fast response, and, the nitrogen risen also can promote oil gas and enter into distillation tower 2, match with the pulling function of vacuum pump set, raise the efficiency and output, oil gas is by entering into condenser 5 after distillation tower 2, enter into after condensation and receive the process that namely oil tank 6 completes an oil product refinement, certainly, in order to strengthen the effect of refining, also the method for making being similar to distilled water can be adopted, adopt two reactors 1, carry out two steaming, improve output and the quality of single sintering.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. a waste mineral oil distillation plant, it is characterized in that, comprise: reactor, distillation tower, outside pipeline road, injection tubing, condenser, receive oil tank, filling tank, heating unit, Nitrogen plant group, vacuum pump set, described distillation tower to be located at above described reactor and to be connected described condenser, described receipts oil tank one end is connected with described condenser by pipeline, the other end is connected with described vacuum pump set by pipeline, described outside pipeline road one end is connected with described filling tank, the other end connects with the injection tubing being positioned at described reactor inside, described heating unit is supplied to described distillation tower and described outside pipeline road heat energy, nitrogen is delivered to described reactor inside by the nitrogen blanketing valve road extending into described reactor inside by described Nitrogen plant group.
2. waste mineral oil distillation plant as described in the appended claim 1, it is characterized in that: described heating unit is the well heater frequently that shakes, comprising shake heater coil, fluid frequently of shake frequently heating unit and the oil gas that is connected electrically to shake heater coil frequently, described oil gas shakes frequently, and heater coil wraps is in described distillation tower periphery, and described fluid shakes frequency heater coil wraps at the described outside pipeline road outer wall of part.
3. waste mineral oil distillation plant as stated in claim 2, is characterized in that: described in the well heater frequently that shakes be induction heating, frequency is 7-20kHz, and heated constant temperature scope is 160-500 DEG C, and temperature control adopts PID to regulate.
4. waste mineral oil distillation plant as described in the appended claim 1, is characterized in that: the opening in described nitrogen blanketing valve road is located at apart from 200-300mm place at the bottom of the still of described reactor, and the opening end in described nitrogen blanketing valve road is provided with and fills nitrogen spiral nozzle.
5. waste mineral oil distillation plant as claimed in claim 4, it is characterized in that: the pipe number of described nitrogen blanketing valve road in described reactor is 2, and caliber is 1/4-1 inch, filling nitrogen flow is 5-20m
3/ h.
6. waste mineral oil distillation plant as described in the appended claim 1, is characterized in that: described injection tubing is detachably provided with several spiral nozzles for oil spout, described spiral nozzle is conical hollow.
7. waste mineral oil distillation plant as recited in claim 6, it is characterized in that: the taper base angle of described spiral nozzle is 60 °, described spiral nozzle fluid area is 1:1.3 ~ 1:1.5 with the ratio of described injection tubing open area.
8. waste mineral oil distillation plant as described in the appended claim 1, it is characterized in that: described reactor is inner, be positioned at below described injection tubing and be provided with gas-liquid phase-splitting net, described gas-liquid phase-splitting net is apart from the still top 600-1000mm of described reactor, described reactor is divided into upper and lower two spaces by described gas-liquid phase-splitting net, wherein, the volumetric ratio of upper space and described reactor is 1:5 ~ 1:3.
9. waste mineral oil distillation plant as claimed in claim 8., is characterized in that: being just provided with oil-air pressure to the part of distillation tower supplements mouth on the net in described gas-liquid phase-splitting, the hole of described oil-air pressure supplements mouth to be diameter be 400-600mm.
10. waste mineral oil distillation plant as described in the appended claim 1, is characterized in that: be also provided with vacuum buffer tank between described receipts oil tank and described vacuum pump set.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410019277.9A CN103756717B (en) | 2014-01-15 | 2014-01-15 | A kind of waste mineral oil distillation plant |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410019277.9A CN103756717B (en) | 2014-01-15 | 2014-01-15 | A kind of waste mineral oil distillation plant |
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| Publication Number | Publication Date |
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| CN103756717A CN103756717A (en) | 2014-04-30 |
| CN103756717B true CN103756717B (en) | 2015-08-26 |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103965952A (en) * | 2014-05-13 | 2014-08-06 | 福州市环天燃料科技有限公司 | Waste oil treatment reaction system |
| CN113332742A (en) * | 2021-06-30 | 2021-09-03 | 张婷娟 | Distillation type separation device for white mineral oil and xylene mixed solution |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4717468A (en) * | 1985-12-23 | 1988-01-05 | Phillips Petroleum Company | Distillation process control for maximum recovery using minimum energy |
| CN202054812U (en) * | 2011-05-06 | 2011-11-30 | 烟台市牟平区留德润滑油销售有限公司 | Distillation equipment for processing waste lubricating oil |
| CN102311754A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Crude oil pressure-reduced distillation method and device |
-
2014
- 2014-01-15 CN CN201410019277.9A patent/CN103756717B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4717468A (en) * | 1985-12-23 | 1988-01-05 | Phillips Petroleum Company | Distillation process control for maximum recovery using minimum energy |
| CN102311754A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Crude oil pressure-reduced distillation method and device |
| CN202054812U (en) * | 2011-05-06 | 2011-11-30 | 烟台市牟平区留德润滑油销售有限公司 | Distillation equipment for processing waste lubricating oil |
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| CN103756717A (en) | 2014-04-30 |
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