CN104293385A - Process for extracting aromatic hydrocarbon oil - Google Patents
Process for extracting aromatic hydrocarbon oil Download PDFInfo
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- CN104293385A CN104293385A CN201310302213.5A CN201310302213A CN104293385A CN 104293385 A CN104293385 A CN 104293385A CN 201310302213 A CN201310302213 A CN 201310302213A CN 104293385 A CN104293385 A CN 104293385A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a process for extracting aromatic hydrocarbon oil. The process comprises the steps: highly aromatic oil and a solvent are in reverse contact in an extraction tower, a refined liquid obtained from the tower top is subjected to solvent removal to obtain an environment-friendly aromatic hydrocarbon oil product; and an extract liquid obtained from the tower bottom is subjected to solvent removal to obtain a by-product rich in polycyclic aromatic hydrocarbons, and the solvent is recovered for recycling. With the conventional rubber filling highly aromatic oil as the raw material, and through the way of solvent refining, the polycyclic aromatic hydrocarbons in the highly aromatic oil are selectively removed, so that the required environment-friendly aromatic hydrocarbon oil product is prepared, and the solvent is recovered for recycling; a pressurized gas phase solvent is used for recovering heat, so that the yield of the environment-friendly aromatic hydrocarbon oil can be effectively improved, the quality of the environment-friendly aromatic hydrocarbon oil is guaranteed, and the recovery cost of the solvent is reduced. The aromatic hydrocarbon oil prepared by the method has benzopyrene less than 1 ppm, has the total amount of 8 types of polycyclic aromatic hydrocarbon compounds less than 10 ppm, fully meets European Union environmental requirements, and has the CA value of 25% or more.
Description
Technical field
The present invention relates to a kind of rubber industry field, be specifically related to a kind of extraction process for the extending oil-aromatic hydrocarbon oil in rubber industry.
Background technology
Rubber filling oil is mainly divided three classes according to the difference of structure: aromatic base, cycloalkyl, paraffinic base, and wherein, aromatic base rubber filling oil is generally got by the furfural extract oil in conventional lubrication oil production process.Aromatic base rubber filling oil is mainly used in the filling in tyre rubber, the rubber trade mark is SBR-1712, but recently because the states such as European Union strengthen the restriction of polycyclic aromatic hydrocarbon content in tire, the tire product making domestic tire production business export to above-mentioned country is faced with huge environmental protection pressure.For solving this environmental issue, simultaneously also for adapting to domestic higher environmental requirement in the future, tire manufacturer and rubber manufacturer start the substitute finding aromatic base rubber filling oil one after another.
A kind of production technique of environment-friendly aromatic oil is proposed in patent CN200810223448.4, the heavy solvent of producing with Lubricating oil refining device extracts oil out for raw material, introduce that density is little, viscosity is little in the feed, the simple substance hydrocarbon of boiling point within the scope of 80 DEG C ~ 300 DEG C or light hydrocarbons auxiliary agent, reduce the viscosity of raw material, increase the density difference of raw material and solvent, improve the selectivity of solvent, thus realize refining the selectivity of raw material, manufactured experimently out that aromatic carbon content is not less than 19.0%, aromaticity content is greater than 50.0%, environmental protection index meets the environment-friendly aromatic oil of European Union requirements.But which introduce the second solvent, add the complicacy of system, and the aromatic carbon content of its environment-friendly aromatic oil is on the low side, fail to reach better requirement (the aromatic carbon content about 25% of environment-friendly aromatic oil).
A kind of production technique of environment-friendly aromatic oil is it is also proposed in patent CN200910050832.3, utilize stock oil fully to contact with difference in specific gravity adverse current in extraction tower of solvent and carry out extracting, polycyclic aromatic hydrocarbons in stock oil is dissolved in solvent, stock oil after extracting carries out solvent recuperation through stripping process, remove the solvent wherein carried secretly, obtain environment-friendly aromatic oil.But in desolvation process, need at ambient pressure through heating for multiple times, solvent removal effect is poor.
At present, the central environment-friendly aromatic oil production preferably of rubber is applied in substantially from heavy arene oil refining, i.e. TDAE.How to improve the yield of TDAE, reducing the energy consumption of whole set process flow process, is the emphasis of current research.
Summary of the invention
The invention provides a kind of processing method meeting the environment-friendly aromatic oil of rubber filling requirement, adopt this technique effectively can improve the yield of environment-friendly aromatic oil, ensure the quality of environment-friendly aromatic oil, and reduce the extraction process of the aromatic hydrocarbon oil of solvent recuperation cost.
Concrete technical scheme of the present invention is as follows:
An extraction process for aromatic hydrocarbon oil, comprises the steps:
(1) high virtue oil enters nitrogen adsorption tower after heating up, and enter extraction tower bottom after contacting with the solvent counter current in nitrogen adsorption tower, contact with the solvent counter current on extraction tower top, raffinate is from extraction tower top discharge, and Extract is from extraction tower bottom discharge;
(2) raffinate that step (1) obtains enters raffinate gas stripping column and carries out nitrogen air lift after being heated to 150-180 DEG C, and the pressure in raffinate gas stripping column is 1 ~ 50kPa, is aromatic hydrocarbon oil from raffinating oil of going out of raffinate gas stripping column tower bottom flow;
(3) Extract that step (1) obtains is carried out heating under reduced pressure, be decompressed to 50-80kPa, be heated to 100-170 DEG C, then carry out gas-liquid separation through flashing tower, the solvent vapo(u)r that flashing tower tower top flows out, through being forced into normal pressure, is back to extraction tower top after cooling together with supplementing solvent; The liquid gone out from flashing tower tower bottom flow enters Extract gas stripping column and carries out nitrogen air lift after heat exchange, and the pressure in Extract gas stripping column is 1 ~ 50kPa, and the extraction oil gone out from tower bottom flow is polycyclic aromatic hydrocarbons oil;
(4) nitrogen adsorption tower is entered from raffinate gas stripping column, the Extract gas stripping column tower top nitrogen carrying solvent out and height virtue oil carries out counter current contact, nitrogen after desolvation escapes into nitrogen drying tower from nitrogen adsorption column overhead, enters raffinate gas stripping column and nitrogen air lift is carried out in Extract gas stripping column bottom from nitrogen drying tower nitrogen out after nitrogen compressor pressurization together with supplementary nitrogen.
Enter nitrogen adsorption tower after high fragrant oil is warming up to 40-60 DEG C in step (1), after contacting with the solvent counter current in nitrogen adsorption tower again with heat exchange of raffinating oil to 70-100 DEG C, then enter extraction tower bottom.
The solvent vapo(u)r that in step (3), flashing tower tower top flows out, through being forced into normal pressure, is back to extraction tower top after being cooled to 70-100 DEG C together with supplementing solvent.
To be forced into through nitrogen compressor from nitrogen drying tower nitrogen out in step (4) and to enter raffinate gas stripping column after 25-50kPa together with supplementary nitrogen and nitrogen air lift is carried out in Extract gas stripping column bottom.
In step (1), the solvent on extraction tower top and the volume ratio of height virtue oil are 0.5 ~ 5:1; Temperature in extraction tower is 40 ~ 110 DEG C, 10 ~ 30 minutes time that high virtue oil stops in extraction tower.The time benefit be selected within the scope of this that temperature in extraction tower and high virtue oil stop in extraction tower be ensure high fragrant oil can fully extracting in solvent.
Described solvent is selected from the one in furfural, phenol, N-Methyl pyrrolidone, N-formyl morpholine, dimethyl sulfoxide (DMSO).
As long as the existing rubber filling of high virtue oil of the present invention with high fragrant oil can, preferably, high fragrant grease separation subtracts three lines from Suizhong 36-1 cycloalkyl and extracts one in the height virtue oil of oil, Taiwan Zhong You company out.
The present invention is oily for raw material with the high virtue of existing rubber filling, by solvent-refined way, optionally the polycyclic aromatic hydrocarbons in the middle of fragrant for height oil is removed, thus obtained required environment-friendly aromatic oil production, solvent recuperation Posterior circle utilizes, and adopts supercharging vapor phase solvent to reclaim heat, effectively can improve the yield of environment-friendly aromatic oil, ensure the quality of environment-friendly aromatic oil, and reduce the cost recovery of solvent.Its benzopyrene of aromatic hydrocarbon oil that the method for the invention obtains is less than 1ppm, and 8 kinds of polycyclic aromatic hydrocarbon compounds total amounts are less than 10ppm, meet the environmental requirement of European Union completely, and CA value is more than 25%.
Accompanying drawing explanation
The process flow sheet of Fig. 1 to be the present invention with two dot chain line be left-half of rupture line;
The process flow sheet of Fig. 2 to be the present invention with two dot chain line be right half part of rupture line.
Embodiment
Describe the present invention below in conjunction with specific embodiment.Protection scope of the present invention is not limited with embodiment, but is limited by claim.
See Fig. 1 and Fig. 2, technical process of the present invention is described in detail.
The extraction process of aromatic hydrocarbon oil of the present invention, comprises the steps:
(1) high virtue oil enters in nitrogen adsorption tower T107 after raw material tank field is heated to 50 DEG C, contact with the solvent counter current in nitrogen adsorption tower T107, solvent absorbing in circulating nitrogen gas is got off, use pump P101(feedstock pump again) pump and enter extraction tower T101 bottom through interchanger E101 with heat exchange to 90 DEG C of raffinating oil, from the circulating solvent of interchanger E109 by extraction tower T101 top charging.High virtue oil contacts with the solvent counter current on extraction tower T101 top, and raffinate is from extraction tower T101 top discharge, and Extract is from extraction tower T101 bottom discharge;
(2) from the raffinate of extraction tower T101 tower top discharging through interchanger E102 heat exchange to 115 DEG C, through interchanger E103 heat exchange to 132 DEG C, again through interchanger E104 heat exchange to 147 DEG C, enter process furnace F101 and be heated to 170 DEG C, enter raffinate gas stripping column T102 and carry out nitrogen air lift, pressure in raffinate gas stripping column T102 is 1 ~ 50kPa, aromatic hydrocarbon oil is from raffinating oil of going out of raffinate gas stripping column T102 tower bottom flow, this aromatic hydrocarbon oil is through interchanger E104 heat exchange to 158 DEG C, again through interchanger E101 heat exchange to 124 DEG C, export after the pump P102 that raffinates oil is forced into normal pressure;
(3) at the bottom of extraction tower T101 tower Extract out through interchanger E105 heat exchange to 102 DEG C, through interchanger E106 heat exchange to 122 DEG C, again through interchanger E107 heat exchange to 156 DEG C, then through being decompressed to 50-80kPa, enter process furnace F102 and be heated to 170 DEG C, enter first flashing tower T103 and carry out gas-liquid separation, liquid at the bottom of first flashing tower T103 tower through interchanger E110 by 131 DEG C of heat exchange to 147 DEG C, enter second flashing tower T104 and carry out gas-liquid separation, at the bottom of second flashing tower T104 tower, liquid is through interchanger E111 heat exchange to 163 DEG C, enter the 3rd flashing tower T105 and carry out gas-liquid separation, at the bottom of 3rd flashing tower T105 tower, liquid is through interchanger E112 heat exchange to 168 DEG C, enter Extract gas stripping column T106 and carry out nitrogen air lift, pressure in Extract gas stripping column is 1 ~ 50kPa, the nitrogen carrying solvent escapes in nitrogen adsorption tower T107 from Extract gas stripping column T106 tower top, the extraction oil gone out from tower bottom flow is polycyclic aromatic hydrocarbons oil, polycyclic aromatic hydrocarbons oil directly exports through extracting out after oil pump P105 is forced into normal pressure,
First flashing tower T103, second flashing tower T104, the 3rd flashing tower T105 tower top solvent vapo(u)r out pressurize through compressor C102, temperature rises to 180 DEG C, through interchanger E112 heat exchange to 179 DEG C, through interchanger E111 heat exchange to 173 DEG C, again through interchanger E110 heat exchange to 157 DEG C, enter gas-liquid separator V101.Liquid bottom gas-liquid separator V101, through interchanger E106 heat exchange to 133 DEG C, through interchanger E102 heat exchange to 126 DEG C, is forced into normal pressure through solvent topping-up pump P103; The solvent vapo(u)r at gas-liquid separator V101 top is warming up to 180 DEG C through compressor C101 pressurization, through interchanger E107 heat exchange to 168 DEG C, through interchanger E103 heat exchange to 158 DEG C, then there is a small amount of steam cooling to 130 DEG C through interchanger E108, be forced into normal pressure through solvent topping-up pump P104.Aforementioned two portions Solvent at Atmospheric Pressure together through interchanger E105 heat exchange to 113 DEG C, then is back to extraction tower T101 top through interchanger E109 water-cooled to 70-100 DEG C together with supplementing solvent;
(4) raffinate gas stripping column T102, the Extract gas stripping column T106 tower top nitrogen carrying solvent out enter nitrogen adsorption tower T107 and height virtue oil carries out counter current contact, nitrogen after desolvation escapes into nitrogen drying tower T108 from nitrogen adsorption tower T107 tower top and removes a small amount of moisture, be forced into 25-50kPa through nitrogen compressor C103 again, then enter raffinate gas stripping column T102 together with supplementary nitrogen, nitrogen air lift is carried out in Extract gas stripping column T106 tower bottom.
In above-mentioned steps (1), the solvent on extraction tower top and the volume ratio of height virtue oil are 0.5 ~ 5:1; Temperature in extraction tower is 40 ~ 110 DEG C, 10 ~ 30 minutes time that high virtue oil stops in extraction tower.Described solvent is selected from the one in furfural, phenol, N-Methyl pyrrolidone, N-formyl morpholine, dimethyl sulfoxide (DMSO).
As long as the existing rubber filling of described height virtue oil with high fragrant oil can, preferably, high fragrant grease separation subtracts three lines from Suizhong 36-1 cycloalkyl and extracts one in the height virtue oil of oil, Taiwan Zhong You company out.
embodiment 1
With the height of Taiwan Zhong You company virtue oil for raw material, dimethyl sulfoxide (DMSO) is solvent, agent-oil ratio (volume ratio refers to dimethyl sulfoxide (DMSO) and height virtue oil volume ratio) 1.0.Aforesaid method is adopted to carry out extracting to the fragrant oil of height, temperature in extraction tower T101 is 90 DEG C, the 15 minutes time that high virtue oil stops in extraction tower, the raffinate obtained from extraction tower T101 top discharge is after raffinate gas stripping column T102 nitrogen air lift, be environment-friendly aromatic oil from raffinating oil of going out of raffinate gas stripping column T102 tower bottom flow, the pressure in raffinate gas stripping column T102 is 50kPa.The Extract obtained from extraction tower T101 bottom discharge is after Extract gas stripping column T106 nitrogen air lift, and the extraction oil gone out from Extract gas stripping column T106 tower bottom flow is polycyclic aromatic hydrocarbons oil, and the pressure in Extract gas stripping column T106 is 20kPa.
embodiment 2
Subtract three lines with Suizhong 36-1 cycloalkyl and extract oil out for raw material, furfural is solvent, agent-oil ratio (volume ratio refers to that furfural and Suizhong 36-1 cycloalkyl subtract the volume ratio that oil extracted out by three lines) 5.Adopt aforesaid method to subtract three lines extraction oil to Suizhong 36-1 cycloalkyl and carry out extracting, temperature in extraction tower T101 is 90 DEG C, Suizhong 36-1 cycloalkyl subtracts three lines and extracts the oily 30 minutes time stopped in extraction tower out, the raffinate obtained from extraction tower T101 top discharge is after raffinate gas stripping column T102 nitrogen air lift, be environment-friendly aromatic oil from raffinating oil of going out of raffinate gas stripping column T102 tower bottom flow, the pressure in raffinate gas stripping column T102 is 25kPa.The Extract obtained from extraction tower T101 bottom discharge is after Extract gas stripping column T106 nitrogen air lift, and the extraction oil gone out from Extract gas stripping column T106 tower bottom flow is polycyclic aromatic hydrocarbons oil, and the pressure in Extract gas stripping column T106 is 50kPa.
embodiment 3
Subtract three lines with Suizhong 36-1 cycloalkyl and extract oil out for raw material, N-Methyl pyrrolidone is solvent, agent-oil ratio (volume ratio refers to that N-Methyl pyrrolidone and Suizhong 36-1 cycloalkyl subtract the volume ratio that oil extracted out by three lines) 3.Adopt aforesaid method to subtract three lines extraction oil to Suizhong 36-1 cycloalkyl and carry out extracting, temperature in extraction tower T101 is 110 DEG C, Suizhong 36-1 cycloalkyl subtracts three lines and extracts the oily 10 minutes time stopped in extraction tower out, the raffinate obtained from extraction tower T101 top discharge is after raffinate gas stripping column T102 nitrogen air lift, be environment-friendly aromatic oil from raffinating oil of going out of raffinate gas stripping column T102 tower bottom flow, the pressure in raffinate gas stripping column T102 is 10kPa.The Extract obtained from extraction tower T101 bottom discharge is after Extract gas stripping column T106 nitrogen air lift, and the extraction oil gone out from Extract gas stripping column T106 tower bottom flow is polycyclic aromatic hydrocarbons oil, and the pressure in Extract gas stripping column T106 is 50kPa.
Aromatic hydrocarbon oil character obtained by each embodiment is as shown in table 1.
The physico-chemical property of the aromatic hydrocarbon oil that each embodiment of table 1 obtains
As can be seen from Table 1, its benzopyrene of aromatic hydrocarbon oil that the method for the invention obtains is less than 1ppm, and 8 kinds of polycyclic aromatic hydrocarbon compounds total amounts are less than 10ppm, meet the environmental requirement of European Union completely, and CA value is more than 25%.Effectively improve the yield of environment-friendly aromatic oil, ensure the quality of environment-friendly aromatic oil.
Claims (7)
1. an extraction process for aromatic hydrocarbon oil, is characterized in that comprising the steps:
(1) high virtue oil enters nitrogen adsorption tower after heating up, and enter extraction tower bottom after contacting with the solvent counter current in nitrogen adsorption tower, contact with the solvent counter current on extraction tower top, raffinate is from extraction tower top discharge, and Extract is from extraction tower bottom discharge;
(2) raffinate that step (1) obtains enters raffinate gas stripping column and carries out nitrogen air lift after being heated to 150-180 DEG C, and the pressure in raffinate gas stripping column is 1 ~ 50kPa, is aromatic hydrocarbon oil from raffinating oil of going out of raffinate gas stripping column tower bottom flow;
(3) Extract that step (1) obtains is carried out heating under reduced pressure, be decompressed to 50-80kPa, be heated to 100-170 DEG C, then carry out gas-liquid separation through flashing tower, the solvent vapo(u)r that flashing tower tower top flows out, through being forced into normal pressure, is back to extraction tower top after cooling together with supplementing solvent; The liquid gone out from flashing tower tower bottom flow enters Extract gas stripping column and carries out nitrogen air lift after heat exchange, and the pressure in Extract gas stripping column is 1 ~ 50kPa, and the extraction oil gone out from tower bottom flow is polycyclic aromatic hydrocarbons oil;
(4) nitrogen adsorption tower is entered from raffinate gas stripping column, the Extract gas stripping column tower top nitrogen carrying solvent out and height virtue oil carries out counter current contact, nitrogen after desolvation escapes into nitrogen drying tower from nitrogen adsorption column overhead, enters raffinate gas stripping column and nitrogen air lift is carried out in Extract gas stripping column bottom from nitrogen drying tower nitrogen out after nitrogen compressor pressurization together with supplementary nitrogen.
2. the extraction process of aromatic hydrocarbon oil according to claim 1, it is characterized in that entering nitrogen adsorption tower after high fragrant oil is warming up to 40-60 DEG C in step (1), after contacting with the solvent counter current in nitrogen adsorption tower again with heat exchange of raffinating oil to 70-100 DEG C, then enter extraction tower bottom.
3. the extraction process of aromatic hydrocarbon oil according to claim 1 and 2, is characterized in that the solvent vapo(u)r of flashing tower tower top outflow in step (3) is through being forced into normal pressure, is back to extraction tower top after being cooled to 70-100 DEG C together with supplementing solvent.
4. the extraction process of aromatic hydrocarbon oil according to claim 3, is characterized in that being forced into from nitrogen drying tower nitrogen out through nitrogen compressor in step (4) entering raffinate gas stripping column after 25-50kPa together with supplementary nitrogen and nitrogen air lift is carried out in Extract gas stripping column bottom.
5. the extraction process of aromatic hydrocarbon oil according to claim 4, is characterized in that the solvent on extraction tower top in step (1) and the volume ratio of height virtue oil are 0.5 ~ 5:1; Temperature in extraction tower is 40 ~ 110 DEG C, 10 ~ 30 minutes time that high virtue oil stops in extraction tower.
6. the extraction process of aromatic hydrocarbon oil according to claim 1, is characterized in that described solvent is selected from the one in furfural, phenol, N-Methyl pyrrolidone, N-formyl morpholine, dimethyl sulfoxide (DMSO).
7. the extraction process of aromatic hydrocarbon oil according to claim 1, is characterized in that described height virtue grease separation subtracts the one in the height virtue oil of three lines extraction oil, Taiwan Zhong You company from Suizhong 36-1 cycloalkyl.
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| CN201310302213.5A CN104293385B (en) | 2013-07-18 | 2013-07-18 | A kind of extraction process of aromatic naphtha |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105754707A (en) * | 2016-03-22 | 2016-07-13 | 中山大学 | Lubricating oil furfural refinement device provided with multi-stage extract recovery system and method |
| CN106221791A (en) * | 2016-08-09 | 2016-12-14 | 兰州石化职业技术学院 | A kind of base oil spent bleaching clay selectivity de-oiling method and device thereof |
| CN108264931A (en) * | 2017-12-25 | 2018-07-10 | 华东理工大学 | For producing the separator of refined bitumen tempered oil |
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| CN101597513A (en) * | 2009-07-14 | 2009-12-09 | 中国海洋石油总公司 | A kind of environment-friendly rubber oil and preparation method thereof |
| CN102146297A (en) * | 2011-03-04 | 2011-08-10 | 苏州久泰集团公司 | Method for producing environmental-friendly aromatic oil |
| CN102643669A (en) * | 2011-02-21 | 2012-08-22 | 中国石油化工股份有限公司 | A production method of low density environment-friendly rubber filling oil |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101597513A (en) * | 2009-07-14 | 2009-12-09 | 中国海洋石油总公司 | A kind of environment-friendly rubber oil and preparation method thereof |
| CN102643669A (en) * | 2011-02-21 | 2012-08-22 | 中国石油化工股份有限公司 | A production method of low density environment-friendly rubber filling oil |
| CN102146297A (en) * | 2011-03-04 | 2011-08-10 | 苏州久泰集团公司 | Method for producing environmental-friendly aromatic oil |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105754707A (en) * | 2016-03-22 | 2016-07-13 | 中山大学 | Lubricating oil furfural refinement device provided with multi-stage extract recovery system and method |
| CN105754707B (en) * | 2016-03-22 | 2018-08-21 | 中山大学 | A kind of lube oil furfural refining unit and method with multistage Extract recovery system |
| CN106221791A (en) * | 2016-08-09 | 2016-12-14 | 兰州石化职业技术学院 | A kind of base oil spent bleaching clay selectivity de-oiling method and device thereof |
| CN106221791B (en) * | 2016-08-09 | 2018-06-08 | 兰州石化职业技术学院 | A kind of base oil spent bleaching clay selectivity de-oiling method and its device |
| CN108264931A (en) * | 2017-12-25 | 2018-07-10 | 华东理工大学 | For producing the separator of refined bitumen tempered oil |
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