CN104178210B - The method and process unit of higher boiling conduction oil are discarded in a kind of recycling - Google Patents
The method and process unit of higher boiling conduction oil are discarded in a kind of recycling Download PDFInfo
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Abstract
A method of higher boiling conduction oil is discarded in recycling, and step has：One, useless conduction oil is pre-processed；Two, hydrofinishing is carried out to the pretreated useless conduction oil of step 1；Three, the useless conduction oil after step 2 hydrofinishing is fractionated, way is：1) from adding the low liquid phase oil branched away of hydrogen to enter vacuum flasher, enter return tank of top of the tower after the mutually condensed device cooling of vacuum flashing tower overhead gas；Gas phase is discharged into air through evacuating, and liquid phase is sent as naphtha to storage tank through the pumped that flows back；2) falling-film distillation the bottomsstream enters vacuum distillation tower after delivery pump pressurizes, enter return tank of top of the tower progress Oil-gas Separation after being evaporated under reduced pressure the condensed device cooling of gas phase of column overhead, liquid phase enters condenser cooling as top oil is subtracted, one is flowed back as column plate, one is delivered to that irrigated area storage tank is personal and export trade as 7# white oils, and one as 15# white oils is delivered to irrigated area storage tank freedom and export trade；With low energy consumption, the characteristics of clean environment firendly, high financial profit and high income.
Description
Technical field
The invention belongs to heat conduction oil recovery techniques fields, and in particular to a method of higher boiling conduction oil is discarded in recycling,
Discarded higher boiling conduction oil is recycled using hight atmospheric molecular distillation technique.
Background technology
Conduction oil is a kind of transfer medium of heat, and since it is with homogeneous heating, temperature adjustment temperature control is accurate, can be in low steam
High temperature is generated under pressure, heat-transfer effect is good, energy saving, the features such as conveying and is easy to operate, is widely used in various fields in recent years
It closes, and its purposes and dosage are more and more.Conduction oil is made due to coking, decomposition etc. under heat conductivility after being used for a long time
Drop, eventually at discarded conduction oil.Discarded conduction oil can be used as fuel oil supply and be used to burnings such as oil plants, but environmental pollution
Greatly, serious waste of resources, and the part of " discarded " only accounts for sub-fraction in discarded conduction oil, it is most of that still there is recycling
Value, is a kind of waste to resource as fuel.
Traditional heat conduction oil recovery method is by discarded oil plant according to acid value acid, alkali chemical treatment adjustment pH value, washing
Later, the absorption such as activated carbon or carclazyte, filtering, drying is added to collect evaporating in a certain temperature range section by vacuum fractionation
Point, reach recycling purpose.This recovery method operating process is long, needs by multiple water-washing process, and will produce acid-base neutralization
The discharge of salt and decolorising agent, clay dregs afterwards, environmental pollution are handed over big.And due to the boiling point of conduction oil height, using rectifying side
Method energy consumption is very big, and product yield is low.In addition, since different types of conduction oil indicator difference is larger, discarding conduction oil has not
Same source, unstable product quality can be also caused using above-mentioned recovery method.
Invention content
In order to overcome the above-mentioned deficiencies of the prior art, the purpose of the present invention is to provide a kind of recycling to discard higher boiling heat conduction
The method of oil has the characteristics of low energy consumption, clean environment firendly, high financial profit and high income.
To achieve the goals above, the technical solution adopted by the present invention is：
A method of higher boiling conduction oil is discarded in recycling, is included the following steps：
One, useless conduction oil is pre-processed, specific practice is：
1) useless conduction oil of different cultivars is sent into drain sump dehydration with vacuum pump by 1250L/H flows, into material temperature
Degree is room temperature, and the useless conduction oil after dehydration, which is divided into two parts into two groups of heat exchangers, to exchange heat：
First part's useless conduction oil exchanges heat with after evaporator fractionation plus hydrogen useless conduction oil component, this portion after heat exchange
Point useless conduction oil enters the gas that evaporator heat exchanger is extracted out with vacuum decompression and exchanges heat, and the temperature of useless conduction oil is big after heat exchange
In 150 DEG C, useless conduction oil goes out falling-film distillation tower and carries out entering distributor after flow-rate adjustment and temperature detection, and first part gives up heat conduction
Hydrogenation component of the oil as two class lubricating oils；
Second part useless conduction oil enters falling-film distillation after being directly entered evaporator heat exchanger and vacuum gas bleeding heat exchange
The heavy constituent (pitch, colloid) of distributor in the middle part of tower, bottom of tower cycle distillation is delivered to irrigated area by pump；
3) useless conduction oil after heat-conducting oil furnace heats step 1) by heating coil is distilled, useless conduction oil temperature control
At 220~300 DEG C, light component distillates system through collector, will be less than being sent into pans after 28 DEG C of component extractings are cooling by flash column,
Heavy constituent accounts for the 75-80% of useless conduction oil charging, and lube base oil and heat conduction oil base oil are done after being handled by fractionating column；
The vacuum pump use water ring-Roots vaccum pump, the vacuum pressure 0.097MPa of vacuum pump, limiting pressure≤
20Pa, speed of exhaust 300L/S~600L/S；
Two, hydrofinishing is carried out to the pretreated useless conduction oil of step 1,
Pretreated hydrogenation component is delivered to hydrogenation plant raw material surge tank, purpose by intermediate storage tank gear wheel metering pump
It is to exchange heat with fractionated products, hydrogenation component is delivered to tank field storage tank by intermediate storage tank pump, and specific practice is：
1) useless conduction oil after the product heat exchanger with Fractionator Bottom being exchanged heat by delivery pump is transported to plus hydrogen surge tank；
2) useless conduction oil in hydrogen surge tank will be added to send to hydrogenation reaction product heat exchanger by metering pump to exchange heat, metering pump
Flow is 500L/H, pressure 16MPa；It is heated to meeting the temperature of process conditions into fused salt electric furnace after mixing with hydrogen
Afterwards, enter hydrogenation protecting reactor, hydrofining reactor according to this, reacted, obtained under the action of desulfurization pour point depression catalyst
To reactor product refined oil；
3) enter high-pressure separator after the heat exchange of reactor product refined oil and useless conduction oil and carry out gas-liquid phase separation, gas is from height
The discharge of separator top is pressed, gas cooling is carried out to 50 DEG C with high pressure hydrogen cooler, cold anticyclone is entered after being mixed with desalted water
Separator (caustic treater), from cold high pressure separator top be discharged hydrogen after recycle hydrogen liquid separation tank gas-liquid separation, then through cycle
Hydrogen compressor send to hydrogen gas compressor preceding pipeline and recycles；Sour water is discharged from cold anticyclone fractionator base, into sewage
System；
4) liquid phase come out from hot high score bottom, low point of heat is entered after pressure is adjusted, and further separation, gas are condensed
High altitude discharge is removed after device cooling, the liquid phase oil come out from hot bottom point bottom is pumped to fractionating column and is fractionated；
Three, the useless conduction oil after step 2 hydrofinishing is fractionated, specific practice is：
1) from adding the low liquid phase oil branched away of hydrogen to enter vacuum flasher, pressure 0.7MPa, 200 DEG C of temperature, flow control
System is heated in 500L/H, the thermal siphon heater of vacuum flashing bottom of tower as auxiliary, and heater heat source is supplied by heat-conducting oil furnace, temperature
Degree is more than 280 DEG C, enters return tank of top of the tower after the mutually condensed device cooling of vacuum flashing tower overhead gas；Gas phase is discharged into air through evacuating,
Liquid phase is delivered to storage tank, the vacuum pressure -0.09MPa of water ring vacuum pump, end vacuum through the pumped that flows back as naphtha
3300Pa, speed of exhaust 115L/S；
2) falling-film distillation the bottomsstream enters vacuum distillation tower after delivery pump pressurizes, and vacuum distillation bottom of tower configures hot rainbow
Heater is inhaled, heater heat source is supplied by heat-conducting oil furnace, and temperature is 280 DEG C, and the condensed device of gas phase for being evaporated under reduced pressure column overhead is cold
But enter return tank of top of the tower afterwards and carry out Oil-gas Separation, gas phase is discharged into air through the extraction of vacuum water ring unit, and Water-ring vacuum unit is empty
Pressure -0.09MPa, end vacuum 3300Pa, speed of exhaust 115L/S, liquid phase are cooled down as top oil is subtracted into condenser, one
It flows back as column plate, one is delivered to that irrigated area storage tank is personal and export trade as 7# white oils, and one as 15# white oils is delivered to irrigated area
Storage tank freedom and export trade；
Falling-film distillation tower the bottomsstream is pressurizeed first by delivery pump as 30# white oils and heat conduction oil base oil and adds hydrogen former
Material oil heat exchanger exchanges heat, and after then being cooled down by product condenser, is conveyed respectively according to mineral oil, synthetic oil different cultivars
To irrigated area storage tank.
The beneficial effects of the invention are as follows：
The present invention due to being recycled in high vacuum conditions using molecular distillation technique, there is an advantage in that：
1) operation temperature low (being far below boiling point), vacuum degree high (zero load≤1Pa), heated time short (in seconds), classification
It is efficient, particularly suitable for higher boiling, the separation of thermal sensitivity, readily oxidizable substance；
2) process for selective hydrogenation, which can be removed effectively, reduces molecular substance (deodorization), weight molecule substance (decoloration) and removing
Impurity in mixture；
3) its separation process is physical separating process, separated object matter can be protected not to be contaminated well, can especially protected
Protecting and leading deep fat takes object to obtain original quality；
4) separation degree is high, and cutting fraction is narrow, is higher than Conventional espresso.
The molecular distillation technique that the present invention uses has operating pressure low, and segregation ratio is high, and low energy consumption, the spy of clean environment firendly
Point, and can more evaporating temperature easily cut into conduction oil raw material to be recycled：Conduction oil, lubricating oil, heavy oil combustion
The Multicomponents such as material improve environment, the economic benefit of product, reprocess and apply valence with very high in terms of discarding conduction oil
Value.
Using the present invention, dispose 20,000 tons of waste minerals oil per year and calculate, can save 1.96 ten thousand tons of petroleum resources, it is per ton can
Generate 12% crude lube stock and 68% conduction oil raw material, 18% high-quality 200# astatkis.
If waste minerals oil is supplied oil plant as fuel material and fuel oil uses enterprise, only 3000 yuan of salvage value per ton
Left and right, processed rear 75~85% component can be used as the raw material use of lubricating oil, hydraulic oil, conduction oil, and value promotion is to often
6500 yuan of ton or more deducts processing charges and loss, the profits tax per ton for about generating 2200 yuan~2700 yuan.
Specific implementation mode
With reference to specific embodiment, invention is further described in detail.
Embodiment
A method of higher boiling conduction oil is discarded in recycling, is included the following steps：
One, useless conduction oil is pre-processed, specific practice is：
1) according to different cultivars, different component, useless conduction oil is from V202, V203, and V503, V601, V602 storage tank are by pumping
P110 is sent into drain sump V1011 dehydrations by 1250L/H flows, and feeding temperature is room temperature, the useless conduction oil after dehydration
It is divided into two parts into two groups of heat exchangers and exchanges heat：
First part's useless conduction oil enters E101, E102 heat exchanger, after being fractionated respectively by T101, T102 evaporator plus hydrogen
Raw material oil ingredient (light component) exchanges heat, this part useless conduction oil after heat exchange enters T102 evaporator heat exchangers and 2# vacuum decompressions
Gas bleeding exchanges heat, and the useless conduction oil temperature after heat exchange is more than 150 DEG C, and useless conduction oil goes out falling-film distillation tower and carries out flow tune
Enter distributor in the middle part of T101 towers, hydrogenation component of first part's useless conduction oil as two class lubricating oils after section and temperature detection；
Second part useless conduction oil, which is directly entered after T101 evaporator heat exchangers exchange heat with 1# vacuum gas bleedings, to be entered
The heavy constituent (pitch, colloid) of distributor in the middle part of T101 towers, bottom of tower cycle distillation is delivered to irrigated area by pump；
2) useless conduction oil after heat-conducting oil furnace heats step 1) by heating coil is distilled, useless conduction oil temperature control
At 220~300 DEG C, light component distillates system through collector, will be less than being sent into pans after 28 DEG C of component extractings are cooling by flash column,
Heavy constituent accounts for the 75-80% of useless conduction oil charging, and lube base oil and heat conduction oil base oil are done after being handled by fractionating column；
The vacuum pump use water ring-Roots vaccum pump, the vacuum pressure 0.097MPa of vacuum pump, limiting pressure≤
20Pa, speed of exhaust 300L/S~600L/S；
Two, to the pretreated useless conduction oil hydrofinishing of step 1, specific practice is：
Pretreated hydrogenation component is delivered to hydrogenation plant raw material surge tank, purpose by intermediate storage tank gear wheel metering pump
It is to exchange heat with fractionated products, hydrogenation component is delivered to tank field V101, V102 storage tank by intermediate storage tank pump, and specific practice is：
1) useless conduction oil after the product heat exchanger E1035 with Fractionator Bottom being exchanged heat by delivery pump is transported to plus hydrogen delays
Rush tank V1025；
2) it is sent to hydrogenation reaction product heat exchanger E1023 and is being exchanged heat by metering pump P1023, P1024, metering pump
The flow 500L/H of P1023, P1024, pressure 16MPa；It is heated to meeting into fused salt electric furnace F1021 after mixing with hydrogen
After the temperature of process conditions, enter hydrogenation protecting reactor R101, hydrofining reactor R102 according to this, is catalyzed in desulfurization pour point depression
It is reacted under the action of agent, obtains reactor product refined oil；
3) enter high-pressure separator V1021 progress gas-liquid phase separations, gas after reactor product refined oil and useless conduction oil heat exchange
Body is discharged from high-pressure separator top, and gas cooling is carried out to 50 DEG C, with desalted water with high pressure hydrogen cooler E1021, E1022
Enter cold high pressure separator (caustic treater) V1023 after mixing, the hydrogen being discharged from cold high pressure separator top is through recycle hydrogen liquid separation
It after tank V1024 gas-liquid separations, then send to device and recycles through circulating hydrogen compressor C102, sour water is arranged from cold high score bottom
Go out, into sewerage；
4) liquid phase come out from the bottoms hot high score V1021, further detaches after pressure is adjusted into low point of V1022 of heat,
High altitude discharge is removed after the condensed device V1026 coolings of gas, the liquid phase oil come out from hot bottom point bottom, which need to be sent to fractionating column fractionation, to be added
Work obtains final products, and hydro-refining unit uses the long-range decentralised controls of DCS, centralized displaying control mode, to the stream in device
Amount, temperature, liquid level, pressure carry out computer programming control；
Three, the useless conduction oil after step 2 hydrofinishing is fractionated, specific practice is：
1) from adding the low liquid phase oil branched away of hydrogen to enter vacuum flasher T1031 by throttle valve flash distillation, pressure is
0.7MPa, 200 DEG C of temperature, flow control add in 500L/H, the thermal siphon heater E1036 of vacuum flashing bottom of tower as auxiliary
Heat, heater heat source are supplied by heat-conducting oil furnace, and temperature is more than 280 DEG C, and vacuum flashing tower overhead gas is mutually cooled down through tower condenser E1031
Enter return tank of top of the tower V1032 afterwards；Gas phase is discharged into air through evacuating, and liquid phase is extracted out through tower top return pump P1031, as naphtha
Device is delivered to irrigated area V1101 storage tanks, water ring vacuum pump B1031 vacuum pressure -0.09MPa, end vacuum 3300Pa, pumping
Rate 115L/S；
2) falling-film distillation the bottomsstream enters vacuum distillation tower T102 after delivery pump P102 pressurizations, is evaporated under reduced pressure bottom of tower
Thermal siphon heater E1037 is configured, heater heat source is supplied by heat-conducting oil furnace, and temperature is 280 DEG C, is evaporated under reduced pressure the gas of column overhead
Mutually enter return tank of top of the tower V1032 after the E1031 coolings of tower condenser and carry out Oil-gas Separation, gas phase is extracted out through vacuum water ring unit
It is discharged into air, two-stage Water-ring vacuum B of Unit 1032 vacuum pressure -0.09MPa, end vacuum 3300Pa, speed of exhaust 115L/S,
Liquid phase is extracted out as top oil is subtracted by delivery pump P1034, P1035, and condenser E1035, E1036 cooling, a difference are respectively enterd
It flows back as column plate, one is delivered to that irrigated area V402 storage tanks are personal and export trade as 7# white oils, and one is delivered to as 15# white oils
Irrigated area V501 storage tanks freedom and export trade；
Falling-film distillation tower the bottomsstream is as 30# white oils and heat conduction oil base oil, by delivery pump P106 pressurizations prior to adding
Hydrogen feedstock oil heat exchanger E1038 exchanges heat, after then being cooled down by product condenser E1039, not according to mineral oil, synthetic oil
It is delivered to that irrigated area V201, V502 storage tank is personal and export trade respectively with kind；Fractionating device uses the long-range decentralised controls of DCS, to dress
Flow, temperature, liquid level, pressure in setting carry out computer programming control.
The oil product of irrigated area storage tank configures
1, V202, V203, V503, V601, V602 storage tank store outsourcing and recycle different types of pretreatment decompression steaming respectively
Evaporate feedstock oil.
2, V101, V102 storage tank, for storing the Hydrogenation raw oil after pretreatment is evaporated under reduced pressure.
3, V103 storage tanks, for storing enterprise's outsourcing, at the heat conduction oil base oil of production different cultivars.
4, V201 storage tanks, for after storing hydrogenation fractionating >=the heat conduction oil base oils (mineral oil) of 330 DEG C of fractions.It both can be with
Personal production conduction oil, and can be with two class lubricating oil base oil export trades.
5, V301 storage tanks, for store pretreatment vacuum distillation after heavy constituent (colloid, asphalitine etc.), be used for export trade and
Personal fuel oil.
6, V302, V401 storage tank, the product conduction oil export trade for storing the different cultivars that enterprise oneself produces.
7, V402 storage tanks, for storing the product 7# white oils after hydrogenation fractionating, for personal and export trade.
8, V501 storage tanks, for storing the product 15# white oils after hydrogenation fractionating, for personal and export trade.
9, V502 storage tanks, for after storing hydrogenation fractionating >=the heat conduction oil base oils (synthetic oil) of 330 DEG C of fractions, you can from
With again can export trade.
10, V1101 storage tanks are mainly used for carrying being processed as organic heat for storing the product naphtha after hydrogenation fractionating
Body system cleaning agent and export trade.
Claims (1)
1. a kind of method that higher boiling conduction oil is discarded in recycling, which is characterized in that include the following steps：
One, useless conduction oil is pre-processed, specific practice is：
1) useless conduction oil of different cultivars is sent into drain sump dehydration with vacuum pump by 1250L/H flows, feeding temperature is
Room temperature, the useless conduction oil after dehydration, which is divided into two parts into two groups of heat exchangers, to exchange heat：
First part's useless conduction oil exchanges heat with after evaporator fractionation plus hydrogen useless conduction oil component, this part after heat exchange is useless
Conduction oil enters the gas that evaporator heat exchanger is extracted out with vacuum decompression and exchanges heat, and the temperature of useless conduction oil is more than after heat exchange
150 DEG C, useless conduction oil, which goes out after falling-film distillation tower carries out flow-rate adjustment and temperature detection, enters distributor, first part's useless conduction oil
Hydrogenation component as two class lubricating oils；
Second part useless conduction oil enters after being directly entered evaporator heat exchanger and vacuum gas bleeding heat exchange in falling-film distillation tower
The heavy constituent of the distributor in portion, bottom of tower cycle distillation is delivered to tank field by pumping；The heavy constituent of the bottom of tower cycle distillation includes drip
Green and colloid；
2) useless conduction oil after heat-conducting oil furnace heats step 1) by heating coil is distilled, and the control of useless conduction oil temperature exists
220~300 DEG C, light component is distillated through collector, be will be less than being sent into pans after 28 DEG C of component extractings are cooling by flash column, be recombinated
Divide the 75-80% for accounting for useless conduction oil charging, lube base oil and heat conduction oil base oil are done after being handled by fractionating column；
The vacuum pump use water ring-Roots vaccum pump, the vacuum pressure 0.097MPa of vacuum pump, limiting pressure≤20Pa,
Speed of exhaust 300L/S~600L/S；
Two, hydrofinishing is carried out to the pretreated useless conduction oil of step 1,
Pretreated hydrogenation component is delivered to hydrogenation plant raw material surge tank by intermediate storage tank gear wheel metering pump, the purpose is to
Fractionated products exchange heat, and hydrogenation component is delivered to tank field storage tank by intermediate storage tank pump, and specific practice is：
1) useless conduction oil after the product heat exchanger with Fractionator Bottom being exchanged heat by delivery pump is transported to plus hydrogen surge tank；
2) useless conduction oil in hydrogen surge tank will be added to send to hydrogenation reaction product heat exchanger by metering pump to exchange heat, the flow of metering pump
For 500L/H, pressure 16MPa；It is heated to after meeting the temperature of process conditions into fused salt electric furnace after being mixed with hydrogen,
Hydrogenation protecting reactor, hydrofining reactor are sequentially entered, is reacted under the action of desulfurization pour point depression catalyst, is obtained anti-
Answer product purification oily；
3) enter high-pressure separator progress gas-liquid phase separation after reactor product refined oil and useless conduction oil heat exchange, gas divides from high pressure
It is discharged from device top, carries out gas cooling to 50 DEG C with high pressure hydrogen cooler, detached into cold anticyclone after being mixed with desalted water
Device, from cold high pressure separator top be discharged hydrogen after recycle hydrogen liquid separation tank gas-liquid separation, then through circulating hydrogen compressor send to
Hydrogen gas compressor preceding pipeline recycles；Sour water is discharged from cold anticyclone fractionator base, into sewerage；The cold height
Pressure separator is caustic treater；
4) liquid phase come out from hot high score bottom, low point of heat is entered after pressure is adjusted, and further separation, the condensed device of gas are cold
But high altitude discharge is removed afterwards, and the liquid phase oil come out from hot bottom point bottom is pumped to fractionating column and is fractionated；
Three, the useless conduction oil after step 2 hydrofinishing is fractionated, specific practice is：
1) from adding the low liquid phase oil branched away of hydrogen to enter vacuum flasher, pressure 0.7MPa, 200 DEG C of temperature, flow control exists
The thermal siphon heater of 500L/H, vacuum flashing bottom of tower are heated as auxiliary, and heater heat source is supplied by heat-conducting oil furnace, and temperature is big
Enter return tank of top of the tower after 280 DEG C, the mutually condensed device cooling of vacuum flashing tower overhead gas；Gas phase is discharged into air, liquid phase through evacuating
Through the pumped that flows back, storage tank, the vacuum pressure -0.09MPa of water ring vacuum pump, end vacuum are delivered to as naphtha
3300Pa, speed of exhaust 115L/S；
2) falling-film distillation the bottomsstream enters vacuum distillation tower after delivery pump pressurizes, and the configuration thermal siphon of vacuum distillation bottom of tower adds
Hot device, heater heat source are supplied by heat-conducting oil furnace, and temperature is 280 DEG C, after being evaporated under reduced pressure the condensed device cooling of gas phase of column overhead
Oil-gas Separation is carried out into return tank of top of the tower, gas phase is discharged into air, Water-ring vacuum unit pneumatics power-through the extraction of vacuum water ring unit
0.09MPa, end vacuum 3300Pa, speed of exhaust 115L/S, liquid phase enter condenser cooling as top oil is subtracted, and one is used as tower
Plate flows back, and one is delivered to that tank field storage tank is personal and export trade as 7# white oils, one as 15# white oils be delivered to tank field storage tank from
With and export trade；
Falling-film distillation tower the bottomsstream is as 30# white oils and heat conduction oil base oil, by delivery pump pressurization elder generation and Hydrogenation raw oil
Heat exchanger exchanges heat, and after then being cooled down by product condenser, tank is delivered to respectively according to mineral oil, synthetic oil different cultivars
Area's storage tank.
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| CN201310199862.7A CN104178210B (en) | 2013-05-27 | 2013-05-27 | The method and process unit of higher boiling conduction oil are discarded in a kind of recycling |
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| CN201310199862.7A CN104178210B (en) | 2013-05-27 | 2013-05-27 | The method and process unit of higher boiling conduction oil are discarded in a kind of recycling |
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| CN106190273A (en) * | 2016-08-18 | 2016-12-07 | 湖南万容科技股份有限公司 | A kind of organic solid waste pyrolysis oil processing means and method |
| CN107815328A (en) * | 2017-12-15 | 2018-03-20 | 重庆方盛净化设备有限公司 | Waste oil regeneration rectifying complexes |
| CN108159722A (en) * | 2017-12-29 | 2018-06-15 | 镇江巨茂分子筛有限公司 | The regeneration method of preparing ethylbenzene from dry gas device conduction oil |
| CN109731560A (en) * | 2019-02-19 | 2019-05-10 | 安徽国孚凤凰科技有限公司 | Silica regeneration deoiler and process after a kind of absorption extracting of Reclaimed Base Oil |
| CN109735365A (en) * | 2019-02-26 | 2019-05-10 | 宁波科元精化有限公司 | A kind of technique that heavy raw oil produces No. 7 white oils |
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| FR2725725B1 (en) * | 1994-10-17 | 1996-12-13 | Inst Francais Du Petrole | PROCESS AND PLANT FOR THE PURIFICATION OF WASTE OILS |
| CN1107109C (en) * | 2000-10-26 | 2003-04-30 | 中国石油化工股份有限公司 | Process for recovering waste oil |
| CN102504933B (en) * | 2011-11-17 | 2013-05-15 | 北京耀锋技术开发中心 | Regeneration method of waste lubricating oil |
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Effective date of registration: 20170907 Address after: 255300, No. 1, outer ring road, northwest of Zhoucun District, Shandong, Zibo Applicant after: Shandong Hengli heat carrier Engineering Co. Ltd. Address before: 255000 No. 299-6 Dongmen Road, Zhoucun District, Shandong, Zibo Applicant before: SHANDONG HENGDAO OIL CHEMICAL CO., LTD. |
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Granted publication date: 20180803 Termination date: 20190527 |