CN110923052B - Distillation recovery device for waste lubricating oil regeneration - Google Patents
Distillation recovery device for waste lubricating oil regeneration Download PDFInfo
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- CN110923052B CN110923052B CN201911244481.XA CN201911244481A CN110923052B CN 110923052 B CN110923052 B CN 110923052B CN 201911244481 A CN201911244481 A CN 201911244481A CN 110923052 B CN110923052 B CN 110923052B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
- C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
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Abstract
The invention relates to a distillation recovery device for waste lubricating oil regeneration, which comprises a raw material tank, a dehydration tower, a heating furnace, a vacuum tower, a stripping tower and an oil-water separator, wherein the raw material tank is connected with a plurality of secondary heat exchangers and a residual oil heat exchanger in series through a raw material oil pump, and the residual oil heat exchanger is connected with the middle part of the dehydration tower; the tower bottom of the dehydration tower is connected with a dehydration bottom pump, the dehydration bottom pump is connected with a plurality of primary heat exchangers in series, the primary heat exchangers are connected with the heating furnace, and the heating furnace is connected with the decompression tower; the multi-line oil collecting tank in the decompression tower is connected with the multi-line buffer tank in the stripping tower, the multi-line buffer tank is connected with a multi-line transfer pump, the multi-line transfer pump is in coupling connection with a primary heat exchanger and a secondary heat exchanger, the secondary heat exchanger is connected with a decompression cooler, and the decompression cooler is connected with a product tank. The distillation recovery device can realize the recovery of the waste lubricating oil with complex components, has low energy consumption and is suitable for industrial mass treatment.
Description
Technical Field
The invention relates to a distillation recovery device for regeneration of waste lubricating oil, and belongs to the technical field of separation.
Background
The lubricating oil is a liquid or semisolid lubricating agent used on various types of automobiles and mechanical equipment to reduce friction and protect machines and workpieces, and mainly plays roles in lubrication, auxiliary cooling, rust prevention, cleaning, sealing, buffering and the like. Lubricating oil is used in almost all mechanical equipment, and the lubricating oil used for a long time often contains impurities such as moisture, mechanical residues, carbon deposit and the like, so that the using effect of the lubricating oil is influenced.
The existing device for recovering the waste lubricating oil is usually only used for filtering or removing peculiar smell, is not suitable for recovering the complex waste lubricating oil and is not suitable for industrial treatment. In reality, impurity components in the waste lubricating oil are complex, the lubricating oil used by different machines is different, the waste lubricating oil is a mixture of lubricating oil of different types, and if a distillation recovery device suitable for industrial treatment and suitable for regeneration of the complex waste lubricating oil can be designed, the distillation recovery device has very important practical value.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides the distillation recovery device for regenerating the waste lubricating oil, which can realize the recovery of the waste lubricating oil with complex components, has low energy consumption and low operation cost and is suitable for industrial large-scale treatment.
The technical scheme for solving the technical problems is as follows: a distillation recovery device for waste lubricating oil regeneration comprises a raw material tank, a dehydration tower, a heating furnace, a decompression tower, a stripping tower and an oil-water separator, wherein the raw material tank is connected with a plurality of secondary heat exchangers in series through a raw material oil pump, the secondary heat exchangers are connected with a residual oil heat exchanger in series, the residual oil heat exchanger is connected with the middle part of the dehydration tower through a pipeline, the top of the dehydration tower is connected with two dehydration condensers through a pipeline, the dehydration condensers are connected with a dehydration vacuum tank through a pipeline, the lower end of the dehydration vacuum tank is connected with the oil-water separator, the upper end of the dehydration vacuum tank is connected with a dehydration vacuum pump through a pipeline, the outlet of the dehydration vacuum pump is connected with the oil-water separator through a pipeline, and the gas pumped out of the dehydration vacuum tank by the dehydration vacuum pump can contain partial non-condensable gas and light components, separating in an oil-water separator;
the tower bottom of the dehydration tower is connected with a dehydration bottom pump, the dehydration bottom pump is connected with a plurality of primary heat exchangers in series through pipelines, the primary heat exchangers are connected with the heating furnace through pipelines, the heating furnace is connected with the middle lower part of the decompression tower through pipelines, the tower top of the decompression tower is connected with two decompression condensers through pipelines, the decompression condensers are connected with a decompression vacuum tank through pipelines, the lower end of the decompression vacuum tank is connected with the oil-water separator, the upper end of the decompression vacuum tank is connected with a decompression vacuum pump through a pipeline, the outlet of the decompression vacuum pump is connected with the oil-water separator through a pipeline, and the gas pumped out of the decompression vacuum tank by the decompression vacuum pump can contain part of non-condensable gas and light components and enters the oil-water separator for separation;
the tower bottom of the vacuum tower is connected with a vacuum bottom pump, the vacuum bottom pump is coupled and connected with the residual oil heat exchanger through a pipeline, the residual oil heat exchanger is connected with a residual oil cooler through a pipeline, the residual oil cooler is connected with a residual oil tank through a pipeline, and the residual oil cooler is connected with the raw material tank through a pipeline;
the inside multi-thread oil trap that is equipped with of decompression tower, the inside multi-thread buffer tank that is equipped with of strip tower, multi-thread oil trap passes through the pipe connection multi-thread buffer tank, multi-thread buffer tank is connected with multi-thread transfer pump, multi-thread transfer pump coupling connection once heat exchanger and secondary heat exchanger, secondary heat exchanger has the decompression cooler through the pipe connection, the decompression cooler has the product jar through the pipe connection, the decompression cooler passes through the pipe connection the head tank.
The invention has the beneficial effects that: (1) the waste lubricating oil is used as raw oil, passes through a plurality of secondary heat exchangers and a residual oil heat exchanger through a raw oil pump, and then enters a dehydration tower for dehydration treatment, and the heat energy at different temperatures can be recovered in the multi-stage heat exchange process, so that the heat energy consumption is reduced; (2) materials at the bottom of the dehydration tower pass through a plurality of primary heat exchangers connected in series and then enter the heating furnace for heating, so that the energy consumption of the heating furnace can be reduced, the treatment capacity of the heating furnace is improved, and the recovery efficiency of waste lubricating oil is improved; (3) the raw oil and the material of the vacuum tower are coupled with the residual oil heat exchanger, and the raw oil and the material in the multi-line buffer tank are coupled with the primary heat exchanger and the secondary heat exchanger, so that the coupling utilization of heat energy is realized, the heat energy is reduced, and the operation cost is reduced; (4) the multi-line oil collecting tank and the multi-line buffer tank are arranged, so that the recovery treatment of the waste lubricating oil with complex components can be realized, and the finished lubricating oil with different types and varieties can be recovered from the waste lubricating oil; (5) the distillation recovery device can realize the recovery of the waste lubricating oil with complex components, has low energy consumption and low operation cost, can continuously operate, and is suitable for industrial large-batch treatment.
On the basis of the technical scheme, the invention can be further improved as follows:
further, the secondary heat exchanger comprises a first-line secondary heat exchanger, a second-line secondary heat exchanger and a third-line secondary heat exchanger, the raw material tank is connected with the first-line secondary heat exchanger through a raw material oil pump, the first-line secondary heat exchanger is connected with the second-line secondary heat exchanger in series through a pipeline, the second-line secondary heat exchanger is connected with the third-line secondary heat exchanger in series through a pipeline, and the third-line secondary heat exchanger is connected with the residual oil heat exchanger in series through a pipeline.
The beneficial effect of adopting the further scheme is that: raw oil passes through a first-line secondary heat exchanger, a second-line secondary heat exchanger, a third-line secondary heat exchanger and a residual oil heat exchanger which are connected in series, so that heat energy of different temperature sections can be recovered, and the energy consumption is low.
Further, the primary heat exchanger comprises a primary heat exchanger and a secondary heat exchanger, the dehydration bottom pump is connected with the primary heat exchanger through a pipeline, the primary heat exchanger is connected with the secondary heat exchanger through a pipeline, and the secondary heat exchanger is connected with the heating furnace through a pipeline.
The beneficial effect of adopting the further scheme is that: the tower bottom material of the dehydration tower enters the heating furnace again through the first-line primary heat exchanger and the second-line primary heat exchanger which are connected in series, so that the load of the heating furnace can be reduced, the heat energy consumption of the heating furnace is reduced, the operation cost is reduced, the treatment capacity of the heating furnace can be improved, and the recovery efficiency of lubricating oil is improved.
Further, the heating furnace comprises a convection chamber and a radiation chamber, the convection chamber is positioned at the upper end of the radiation chamber, the primary heat exchanger is connected with the convection chamber through a pipeline, and the radiation chamber is connected with the decompression tower through a pipeline.
The beneficial effect of adopting the further scheme is that: flue gas in a workshop is adopted for heating in the convection chamber, and waste heat is fully utilized, so that the investment of heat energy in the whole process flow is reduced, and the operation cost is reduced.
Furthermore, the multi-line oil collecting tank in the decompression tower comprises a first-line oil collecting tank, a second-line oil collecting tank, a third-line oil collecting tank and a flushing oil collecting tank, the multi-line buffer tank comprises a first-line coke storage tank, a second-line buffer tank, a third-line buffer tank and a first-line buffer tank, the multi-line transfer pump comprises a first-line reduction pump, a second-line reduction pump and a third-line reduction pump, the decompression cooler comprises a first-line reduction cooler, a second-line reduction cooler and a third-line reduction cooler, the primary heat exchanger comprises a first-line primary heat exchanger and a second-line primary heat exchanger, the secondary heat exchanger comprises a first-line secondary heat exchanger, a second-line secondary heat exchanger and a third-line secondary heat exchanger, and the product tank comprises a first product tank, a second product tank and a third product tank;
the first-line oil collecting tank is connected with the first-line coke storage tank through a pipeline, the first-line coke storage tank is connected with the first-line buffer tank through a pipeline, the first-line buffer tank is connected with the first-line subtracting pump, the first-line subtracting pump is connected with the first-line primary heat exchanger through a pipeline coupling, the first-line primary heat exchanger is connected with the first-line secondary heat exchanger in series, the first-line secondary heat exchanger is connected with the first-line subtracting cooler through a pipeline, the first-line subtracting cooler is connected with the first product tank through a pipeline, and the first-line subtracting cooler is connected with the raw material tank through a pipeline;
the second-line oil collecting tank is connected with the second-line buffer tank through a pipeline, the second-line buffer tank is connected with the second-line reduction pump, the outlet of the second-line reduction pump is connected with the second-line primary heat exchanger through a pipeline in a coupling mode, the second-line primary heat exchanger is connected with the second-line secondary heat exchanger in series, the second-line secondary heat exchanger is connected with the second-line reduction cooler through a pipeline, the second-line reduction cooler is connected with the second product tank through a pipeline, and the second-line reduction cooler is connected with the raw material tank through a pipeline;
the flushing oil collecting tank is connected with the three-wire buffer tank through a pipeline, the three-wire buffer tank is connected with the three-wire reduction pump, an outlet of the three-wire reduction pump is connected with the three-wire secondary heat exchanger through a pipeline in a coupling mode, the three-wire secondary heat exchanger is connected with the three-wire reduction cooler through a pipeline, the three-wire reduction cooler is connected with the three product tanks through pipelines, and the three-wire reduction cooler is connected with the raw material tank through a pipeline.
The beneficial effect of adopting the further scheme is that: the inside multi-thread oil catch bowl that is equipped with of decompression tower is equipped with multi-thread buffer tank in the tower, can separate out the lubricating oil finished product of three kinds of different boiling points, and the lubricating oil quality that obtains moreover is higher, does not contain other impurity, can satisfy used repeatedly's demand. The materials in the first line oil collecting tank enter the first line coke storage tank firstly and then enter the first line buffer tank, so that a small amount of non-gel in the materials can be left in the first line coke storage tank, and the problem that the quality of the lubricating oil in the first tank of the product is influenced by the fact that the non-gel enters the first line buffer tank is avoided.
Further, the outlet of the second-line reducing pump is connected with the three-line oil collecting tank through a pipeline, and the outlet of the third-line reducing pump is connected with the flushing oil collecting tank through a pipeline.
The beneficial effect of adopting the further scheme is that: the outlet of the two-line pump is connected with the three-line oil collecting tank through the pipeline, so that part of lubricating oil can flow back to the three-line oil collecting tank again, the filler in the three-line oil collecting tank is washed away, and the blockage caused by excessive impurity accumulation is avoided; the flushing oil collecting tank is located at the lowest part of the decompression tower, heavy component impurities are easy to accumulate, and the outlet of the three-way reducing pump is connected with the flushing oil collecting tank through a pipeline, so that the flushing effect on the filler in the flushing oil collecting tank can be achieved.
Further, the first-line secondary heat exchanger is connected with the top of the vacuum tower through a reflux pipeline, and the first-line cooler is connected with the top of the vacuum tower through a reflux pipeline;
the outlet of the second-line heat exchanger is connected with the top of the vacuum tower through a reflux pipeline, and the second-line secondary heat exchanger is connected with the top of the vacuum tower through a reflux pipeline.
The beneficial effect of adopting the further scheme is that: the reflux of hot materials and the reflux of cold materials are realized, the temperature in the vacuum tower can be effectively controlled, and the over-high or over-low temperature in the vacuum tower is avoided, so that the recovery and distillation process of the waste lubricating oil is stably carried out, and the continuous process flow is ensured; in addition, the extraction rate of the finished lubricating oil can be controlled, and the recovered lubricating oil can meet the quality requirement.
Further, a gas phase pipeline is connected between the first line oil collecting tank and the first line coke storage tank; a gas phase pipeline is connected between the second-line oil collecting tank and the second-line buffer tank; and a gas phase pipeline is connected between the flushing oil collecting tank and the three-line buffer tank.
The beneficial effect of adopting the further scheme is that: the arrangement of the gas phase pipeline can ensure that the air pressure between the first line oil collecting tank and the first line coke storage tank, between the second line oil collecting tank and the second line buffer tank and between the flushing oil collecting tank and the third line buffer tank is balanced, so that the material transfer between the pressure reducing tower and the stripping tower is smoother, and the continuous operation of the recovery process flow of the waste lubricating oil is ensured.
Further, a vent is arranged at the upper end of the oil-water separator, a non-condensable gas pipeline is arranged at the upper end of the oil-water separator, and the non-condensable gas pipeline is connected with the heating furnace; the lower end of the oil-water separator is connected with a light oil pump, and the light oil pump is connected with a light oil tank through a pipeline; the oil-water separator lower extreme is connected with circulating water pump, the export of circulating water pump is through pipeline connection sewage treatment workshop of the same kind, the export of circulating water pump has two moisturizing coolers through another way pipeline connection, the moisturizing cooler passes through the pipe connection dehydration vacuum pump and decompression vacuum pump.
The beneficial effect of adopting the further scheme is that: the arrangement of the vent can avoid danger caused by pressure building in the oil-water separator; the arrangement of the non-condensable gas pipeline can ensure that the non-condensable gas in the oil-water separator enters the heating furnace for utilization, thereby saving heat energy; the arrangement of the circulating water pump and the water supplementing cooler can realize better separation of the light oil and the water.
Drawings
FIG. 1 is a schematic view of the distillation recovery apparatus in the example;
FIG. 2 is a schematic view of the structure of the heating furnace in the embodiment;
FIG. 3 is a schematic structural view of the vacuum column and the stripping column in the example;
FIG. 4 is a schematic structural diagram of the oil-water separator in the embodiment;
in the figure, a T201 dehydrating tower, an F201 heating furnace, a T202 vacuum tower, a T203 stripping tower, a V203 oil-water separator, a P103 raw material oil pump, an E204 residual oil heat exchanger, an E207 dehydrating condenser, a V201 dehydrating vacuum tank, a P208 dehydrating vacuum pump, a P201A/B dehydrating bottom pump, an E213 vacuum condenser, a V202 vacuum tank, a P207 decompressing vacuum pump, a P202A/B decompressing bottom pump, an E212 residual oil cooler, an E201B one-line secondary heat exchanger, an E202B two-line secondary heat exchanger, an E203 three-line secondary heat exchanger, an E201A one-line primary heat exchanger, an E202A two-line primary heat exchanger, an F201-1 convection chamber, an F201-2 radiation chamber, a T202-1 one-line oil collecting tank, a T202-2 two-line oil collecting tank, a T202-3 three-line oil collecting tank, a T202-4 flushing oil collecting tank, a T203-1 one-line coke collecting tank, a T203-2 two-line buffer tank, a T203-3 one-line buffer tank, a T203-4 three line buffer tank, a P206A/B minus first-line pump, a P205A/B minus second-line pump, a P203A/B minus third-line pump, an E208 minus first-line cooler, an E209 minus second-line cooler, an E211 minus third-line cooler, a P210 light oil pump, a P209 circulating water pump, and an E206 water replenishing cooler; 1 gas phase pipeline, 2 vent, 3 noncondensable gas pipeline.
Detailed Description
The present invention will be described in detail with reference to the following embodiments in order to make the aforementioned objects, features and advantages of the invention more comprehensible. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.
As shown in the figure, the distillation recovery device for the regeneration of the waste lubricating oil comprises a raw material tank, a dehydration tower T201, a heating furnace F201, a decompression tower T202, a stripping tower T203 and an oil-water separator V203, the raw material tank is connected with a plurality of secondary heat exchangers in series through a raw material oil pump P103, the secondary heat exchangers are connected with a residual oil heat exchanger E204 in series, the residual oil heat exchanger E204 is connected with the middle part of the dehydrating tower T201 through a pipeline, the top of the dehydrating tower T201 is connected with two dehydrating condensers E207 through a pipeline, the two dehydration condensers E207 are shown as E207A and E207B, respectively, said dehydration condenser E207 being connected by means of a pipeline to a dehydration vacuum tank V201, the lower end of the dehydration vacuum tank V201 is connected with the oil-water separator V203, the upper end of the dehydration vacuum tank V201 is connected with a dehydration vacuum pump P208 through a pipeline, the outlet of the dehydration vacuum pump P208 is connected with the oil-water separator V203 through a pipeline;
the bottom of the dehydration tower T201 is connected with a dehydration bottom pump P201A/B, the dehydration bottom pump P201A/B is connected with a plurality of primary heat exchangers in series through pipelines, the primary heat exchangers are connected with the heating furnace F201 through pipelines, the heating furnace F201 is connected with the middle lower part of the decompression tower T202 through pipelines, the top of the decompression tower T202 is connected with two decompression condensers E213 through pipelines, the two decompression condensers E213 in the figure are respectively E213A and E213B, the decompression condenser E213 is connected with a decompression vacuum tank V202 through pipelines, the lower end of the decompression vacuum tank V202 is connected with the oil-water separator V203, the upper end of the decompression vacuum tank V202 is connected with a decompression vacuum pump P207 through a pipeline, the outlet of the decompression vacuum pump P207 is connected with the oil-water separator V203 through a pipeline, and the decompression vacuum pump P207 is provided with two condensers P207A and P207B;
a vacuum bottom pump P202A/B is connected to the bottom of the vacuum tower T202, the vacuum bottom pump P202A/B is connected with the residual oil heat exchanger E204 through a pipeline in a coupling mode, the residual oil heat exchanger E204 is connected with a residual oil cooler E212 through a pipeline, the residual oil cooler E212 is connected with a residual oil tank through a pipeline, and the residual oil cooler E212 is connected with the raw material tank through a pipeline;
the inside multi-thread oil trap that is equipped with of decompression tower T202, the inside multi-thread buffer tank that is equipped with of strip tower T203, multi-thread oil trap passes through the pipe connection multi-thread buffer tank, multi-thread buffer tank is connected with multi-thread transfer pump, multi-thread transfer pump coupling connection once heat exchanger and secondary heat exchanger, secondary heat exchanger has the decompression cooler through the pipe connection, the decompression cooler has the product jar through the pipe connection, the decompression cooler passes through the pipe connection the head tank.
The secondary heat exchanger comprises a primary heat exchanger E201B, a secondary heat exchanger E202B and a three-line secondary heat exchanger E203, the raw material tank is connected with the primary heat exchanger E201B through a raw material oil pump P103, the primary heat exchanger E201B is connected with the secondary heat exchanger E202B in series through a pipeline, the secondary heat exchanger E202B is connected with the three-line secondary heat exchanger E203 in series through a pipeline, and the three-line secondary heat exchanger E203 is connected with the residual oil heat exchanger E204 in series through a pipeline.
The primary heat exchanger comprises a primary heat exchanger E201A and a secondary heat exchanger E202A, the dehydration bottom pump P201A/B is connected with the primary heat exchanger E201A through a pipeline, the primary heat exchanger E201A is connected with the secondary heat exchanger E202A through a pipeline, and the secondary heat exchanger E202A is connected with the heating furnace F201 through a pipeline.
The heating furnace F201 comprises a convection chamber F201-1 and a radiation chamber F201-2, the convection chamber F201-1 is positioned at the upper end of the radiation chamber F201-2, the primary heat exchanger is connected with the convection chamber F201-1 through a pipeline, and the radiation chamber F201-2 is connected with the decompression tower T202 through a pipeline.
The multi-line oil collecting tank inside the pressure reducing tower T202 comprises a first line oil collecting tank T202-1, a second line oil collecting tank T202-2, a third line oil collecting tank T202-3 and a flushing oil collecting tank T202-4, the multi-line buffer tank comprises a first line coke storage tank T203-1, a second line buffer tank T203-2, a third line buffer tank T203-4 and a first line buffer tank T203-3, the multi-line transfer pump comprises a first line reducing pump P206A/B, a second line reducing pump P205A/B and a third line reducing pump P203A/B, the pressure reducing cooler comprises a first line reducing cooler E208, a second line cooler E209 and a third line cooler E211, the primary heat exchanger comprises a first line primary heat exchanger E201A and a second line primary heat exchanger E202A, the secondary heat exchanger comprises a first line secondary heat exchanger E201B, a second line secondary heat exchanger E202B and a third line secondary heat exchanger E203, and the product tank comprises a first product tank, a second line oil collecting tank T202 and a flushing oil collecting tank T202-4, A product second tank and a product third tank;
the first-line oil collecting tank T202-1 is connected with the first-line coke storage tank T203-1 through a pipeline, the first-line coke storage tank T203-1 is connected with the first-line buffer tank T203-3 through a pipeline, the first-line buffer tank T203-3 is connected with the first-line reducing pump P206A/B, the first-line reducing pump P206A/B is connected with the first-line primary heat exchanger E201A through a pipeline coupling, the first-line primary heat exchanger E201A is connected with the first-line secondary heat exchanger E201B in series, the first-line secondary heat exchanger E201B is connected with the first-line reducing cooler E208 through a pipeline, the first-line reducing cooler E208 is connected with the first product tank through a pipeline, and the first-line reducing cooler E208 is connected with the raw material tank through a pipeline;
the second-line oil collecting tank T202-2 is connected with the second-line buffer tank T203-2 through a pipeline, the second-line buffer tank T203-2 is connected with the second-line reducing pump P205A/B, the outlet of the second-line reducing pump P205A/B is connected with the second-line primary heat exchanger E202A through a pipeline coupling, the second-line primary heat exchanger E202A is connected with the second-line secondary heat exchanger E202B in series, the second-line secondary heat exchanger E202B is connected with the second-line reducing cooler E209 through a pipeline, the second-line reducing cooler E209 is connected with the second product tank through a pipeline, and the second-line reducing cooler E209 is connected with the raw material tank through a pipeline;
the flushing oil collecting tank T202-4 is connected with the three-wire buffer tank T203-4 through a pipeline, the three-wire buffer tank T203-4 is connected with the three-wire reduction pump P203A/B, the outlet of the three-wire reduction pump P203A/B is connected with the three-wire secondary heat exchanger E203 through a pipeline coupling, the three-wire secondary heat exchanger E203 is connected with the three-wire reduction cooler E211 through a pipeline, the three-wire reduction cooler E211 is connected with the three product tanks through pipelines, and the three-wire reduction cooler E211 is connected with the raw material tank through a pipeline.
The outlet of the three-line reduction pump P205A/B is connected to the three-line sump T202-3 by a pipeline, and the outlet of the three-line reduction pump P203A/B is connected to the flushing sump T202-4 by a pipeline.
The one-line secondary heat exchanger E201B is connected with the top of the vacuum tower T202 through a reflux line, and the minus one-line cooler E208 is connected with the top of the vacuum tower T202 through a reflux line;
the outlet of the second-line reducing pump P205A/B is connected to the top of the vacuum tower T202 through a reflux line, and the second-line secondary heat exchanger E202B is connected to the top of the vacuum tower T202 through a reflux line.
A gas phase pipeline 1 is connected between the first-line oil collecting tank T202-1 and the first-line coke storage tank T203-1; a gas phase pipeline 1 is connected between the second-line oil collecting tank T202-2 and the second-line buffer tank T203-2; and a gas phase pipeline 1 is connected between the flushing oil collecting tank T202-4 and the three-line buffer tank T203-4.
The upper end of the oil-water separator V203 is provided with a vent 2, the upper end of the oil-water separator V203 is provided with a non-condensable gas pipeline 3, and the non-condensable gas pipeline 3 is connected with the heating furnace F201; the lower end of the oil-water separator V203 is connected with a light oil pump P210, and the light oil pump P210 is connected with a light oil tank through a pipeline; the oil water separator V203 lower extreme is connected with circulating water pump P209, and circulating water pump P209 in the picture is equipped with two and is P209A and P209B respectively, the export of circulating water pump P209 is through pipeline connection sewage treatment plant all the way, the export of circulating water pump P209 is through another way pipeline connection have two moisturizing coolers E206, and two moisturizing coolers in the picture are E206A and E206B respectively, moisturizing cooler E206 is through pipeline connection dehydration vacuum pump P208 and decompression vacuum pump P207.
The working principle is as follows: the raw material tank is filled with waste lubricating oil to be regenerated, the raw material pump preheats the waste lubricating oil raw material in the raw material tank sequentially through a first-line secondary heat exchanger E201B, a second-line secondary heat exchanger E202B, a third-line secondary heat exchanger E203 and a residual oil heat exchanger E204, the waste lubricating oil raw material enters a dehydration tower T201 to be subjected to moisture removal, moisture and light oil impurities in the waste lubricating oil are extracted from the top of the dehydration tower T201, and the water and the light oil removed are introduced into an oil-water separator V203 after the condensation action of a dehydration condenser E207; the tower bottom components of the dehydration tower T201 enter a heating furnace F201 for reheating after heat exchange of a first-line primary heat exchanger E201A and a second-line primary heat exchanger E202A, then enter a decompression tower T202 for processing, the materials in a first-line oil collecting tank T202-1 in the decompression tower T202 enter a first-line coke storage tank T203-1, then enter a first-line buffer tank T203-3 for processing, are extracted by a first-line reduction pump P206A/B, enter a first product tank after cooling, and are recovered to obtain one type of lubricating oil product; after materials in a second-line oil collecting tank T202-2 in the decompression tower T202 enter a second-line buffer tank T203-2 to be treated, the materials are collected by a second-line reduction pump P205A/B, and the materials enter a second product tank after being cooled, and the lubricating oil products of another type are obtained through recovery; the materials in the three-line oil collecting tank T202-3 in the decompression tower T202 firstly enter the flushing oil collecting tank T202-4, then enter the three-line buffer tank T203-4 for treatment, are extracted by the three-line reduction pump P203A/B, enter the three product tanks after being cooled, and are recovered to obtain the lubricating oil product of the third type.
The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.
The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.
Claims (7)
1. The distillation recovery device for waste lubricating oil regeneration is characterized by comprising a raw material tank, a dehydration tower (T201), a heating furnace (F201), a vacuum tower (T202), a stripping tower (T203) and an oil-water separator (V203), wherein the raw material tank is connected with a plurality of secondary heat exchangers in series through a raw material oil pump (P103), the secondary heat exchangers are connected with a residual oil heat exchanger (E204) in series, the residual oil heat exchanger (E204) is connected with the middle part of the dehydration tower (T201) through a pipeline, the top of the dehydration tower (T201) is connected with two dehydration condensers (E207) through a pipeline, the dehydration condensers (E207) are connected with a dehydration vacuum tank (V201) through a pipeline, the lower end of the dehydration vacuum tank (V201) is connected with the oil-water separator (V203), the upper end of the dehydration vacuum tank (V201) is connected with a dehydration vacuum pump (P208) through a pipeline, the outlet of the dehydration vacuum pump (P208) is connected with the oil-water separator (V203) through a pipeline;
the bottom of the dehydration tower (T201) is connected with a dehydration bottom pump (P201A/B), the dehydration bottom pump (P201A/B) is connected with a plurality of primary heat exchangers in series through pipelines, the primary heat exchangers are connected with the heating furnace (F201) through pipelines, the heating furnace (F201) is connected with the middle lower part of the decompression tower (T202) through pipelines, the top of the decompression tower (T202) is connected with two decompression condensers (E213) through pipelines, the decompression condensers (E213) are connected with a decompression vacuum tank (V202) through pipelines, the lower end of the decompression vacuum tank (V202) is connected with the oil-water separator (V203), the upper end of the decompression vacuum tank (V202) is connected with a decompression vacuum pump (P207) through pipelines, and the outlet of the decompression vacuum pump (P207) is connected with the oil-water separator (V203) through pipelines;
a vacuum bottom pump (P202A/B) is connected to the bottom of the vacuum tower (T202), the vacuum bottom pump (P202A/B) is connected with the residual oil heat exchanger (E204) through a pipeline in a coupling mode, the residual oil heat exchanger (E204) is connected with a residual oil cooler (E212) through a pipeline, the residual oil cooler (E212) is connected with a residual oil tank through a pipeline, and the residual oil cooler (E212) is connected with the raw material tank through a pipeline;
a multi-line oil collecting tank is arranged in the decompression tower (T202), a multi-line buffer tank is arranged in the stripping tower (T203), the multi-line oil collecting tank is connected with the multi-line buffer tank through a pipeline, the multi-line buffer tank is connected with a multi-line transfer pump, the multi-line transfer pump is in coupling connection with the primary heat exchanger and the secondary heat exchanger, the secondary heat exchanger is connected with a decompression cooler through a pipeline, the decompression cooler is connected with a product tank through a pipeline, and the decompression cooler is connected with the raw material tank through a pipeline;
the multi-line oil collecting tank inside the pressure reducing tower (T202) comprises a first line oil collecting tank (T202-1), a second line oil collecting tank (T202-2), a third line oil collecting tank (T202-3) and a flushing oil collecting tank (T202-4), the multi-line buffer tank comprises a first line coke storage tank (T203-1), a second line buffer tank (T203-2), a third line buffer tank (T203-4) and a first line buffer tank (T203-3), the multi-line transfer pump comprises a first line reducing pump (P206A/B), a second line reducing pump (P205A/B) and a third line reducing pump (P203A/B), the pressure reducing cooler comprises a first line reducing cooler (E208), a second line reducing cooler (E209) and a third line reducing cooler (E211), the first heat exchanger comprises a first line primary heat exchanger (E201A) and a second line primary heat exchanger (E202A), and the second heat exchanger comprises a first line secondary heat exchanger (E201B), A second-line secondary heat exchanger (E202B) and a third-line secondary heat exchanger (E203), wherein the product tank comprises a first product tank, a second product tank and a third product tank;
the first line oil collecting tank (T202-1) is connected with the first line coke storage tank (T203-1) through a pipeline, the first line coke storage tank (T203-1) is connected with the first line buffer tank (T203-3) through a pipeline, the first line buffer tank (T203-3) is connected with the first line pump (P206A/B), the first line pump (P206A/B) is connected with the first line primary heat exchanger (E201A) through a pipeline coupling, the first line primary heat exchanger (E201A) is connected with the first line secondary heat exchanger (E201B) in series, the first line secondary heat exchanger (E201B) is connected with the first line cooler (E208) through a pipeline, the first line cooler (E208) is connected with the first product tank through a pipeline, and the first line cooler (E208) is connected with the raw material tank through a pipeline;
the second-line oil collecting tank (T202-2) is connected with the second-line buffer tank (T203-2) through a pipeline, the second-line buffer tank (T203-2) is connected with the second-line reduction pump (P205A/B), the outlet of the second-line reduction pump (P205A/B) is connected with the second-line primary heat exchanger (E202A) through a pipeline coupling, the second-line primary heat exchanger (E202A) is connected with the second-line secondary heat exchanger (E202B) in series, the second-line secondary heat exchanger (E202B) is connected with the second-line reduction cooler (E209) through a pipeline, the second-line reduction cooler (E209) is connected with the second product tank through a pipeline, and the second-line reduction cooler (E209) is connected with the raw material tank through a pipeline;
the flushing oil collecting tank (T202-4) is connected with the three-wire buffer tank (T203-4) through a pipeline, the three-wire buffer tank (T203-4) is connected with the three-wire reduction pump (P203A/B), the outlet of the three-wire reduction pump (P203A/B) is connected with the three-wire secondary heat exchanger (E203) through a pipeline coupling, the three-wire secondary heat exchanger (E203) is connected with the three-wire reduction cooler (E211) through a pipeline, the three-wire reduction cooler (E211) is connected with the three product tanks through a pipeline, and the three-wire reduction cooler (E211) is connected with the raw material tank through a pipeline;
the outlet of the three-line reduction pump (P205A/B) is connected with the three-line oil collecting tank (T202-3) through a pipeline, and the outlet of the three-line reduction pump (P203A/B) is connected with the flushing oil collecting tank (T202-4) through a pipeline.
2. The apparatus for distillation recovery for spent lubricating oil regeneration according to claim 1, wherein the secondary heat exchanger comprises a primary secondary heat exchanger (E201B), a secondary heat exchanger (E202B) and a three-line secondary heat exchanger (E203), the feed tank is connected to the primary secondary heat exchanger (E201B) through a feed oil pump (P103), the primary secondary heat exchanger (E201B) is connected in series to the secondary heat exchanger (E202B) through a pipeline, the secondary heat exchanger (E202B) is connected in series to the three-line secondary heat exchanger (E203) through a pipeline, and the three-line secondary heat exchanger (E203) is connected in series to the residual oil heat exchanger (E204) through a pipeline.
3. The apparatus for distillation recovery for spent lubricating oil regeneration according to claim 1, wherein the primary heat exchanger comprises a primary heat exchanger (E201A) of one line and a primary heat exchanger (E202A) of two lines, the dehydration bottom pump (P201A/B) is connected to the primary heat exchanger (E201A) of one line through a pipeline, the primary heat exchanger (E201A) of one line is connected to the primary heat exchanger (E202A) of two lines through a pipeline, and the primary heat exchanger (E202A) of two lines is connected to the heating furnace (F201) through a pipeline.
4. The apparatus for distillation recovery of spent lubricating oil according to claim 1, wherein the heating furnace (F201) comprises a convection chamber (F201-1) and a radiation chamber (F201-2), the convection chamber (F201-1) is located at the upper end of the radiation chamber (F201-2), the primary heat exchanger is connected to the convection chamber (F201-1) through a pipeline, and the radiation chamber (F201-2) is connected to the decompression tower (T202) through a pipeline.
5. The apparatus for distillation recovery of spent lubricating oil according to claim 1, wherein the first-line secondary heat exchanger (E201B) is connected to the top of the vacuum tower (T202) through a reflux line, and the minus-one-line cooler (E208) is connected to the top of the vacuum tower (T202) through a reflux line;
the outlet of the two-line-reducing pump (P205A/B) is connected with the top of the vacuum tower (T202) through a reflux line, and the two-line secondary heat exchanger (E202B) is connected with the top of the vacuum tower (T202) through a reflux line.
6. The distillation recovery device for spent lubricating oil regeneration according to claim 1, wherein a gas phase pipeline (1) is connected between the first line oil sump (T202-1) and the first line coke storage tank (T203-1); a gas phase pipeline (1) is connected between the second-line oil collecting tank (T202-2) and the second-line buffer tank (T203-2); and a gas phase pipeline (1) is connected between the flushing oil collecting tank (T202-4) and the three-line buffer tank (T203-4).
7. The distillation recovery device for the regeneration of waste lubricating oil according to claim 1, characterized in that the upper end of the oil-water separator (V203) is provided with a vent (2), the upper end of the oil-water separator (V203) is provided with a noncondensable gas pipeline (3), and the noncondensable gas pipeline (3) is connected with the heating furnace (F201); the lower end of the oil-water separator (V203) is connected with a light oil pump (P210), and the light oil pump (P210) is connected with a light oil tank through a pipeline; oil water separator (V203) lower extreme is connected with circulating water pump (P209), the export of circulating water pump (P209) is through pipeline connection sewage treatment workshop all the way, the export of circulating water pump (P209) has two moisturizing coolers (E206) through another pipeline connection, moisturizing cooler (E206) are through the pipe connection dehydration vacuum pump (P208) and decompression vacuum pump (P207).
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