CN104531209A - Process for improving foaming tendency of waste oil refining process - Google Patents
Process for improving foaming tendency of waste oil refining process Download PDFInfo
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- CN104531209A CN104531209A CN201410686439.4A CN201410686439A CN104531209A CN 104531209 A CN104531209 A CN 104531209A CN 201410686439 A CN201410686439 A CN 201410686439A CN 104531209 A CN104531209 A CN 104531209A
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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
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
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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)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Lubricants (AREA)
- Developing Agents For Electrophotography (AREA)
Abstract
The invention relates to a process for improving foaming tendency of a waste oil refining process, the process mainly includes furfural refining, first carclazyte refining, adsorption refining and secondary carclazyte refining; a filtered oil product obtained by first refining is adsorbed and refined by an adsorbent, then carclazyte refining is performed, and after the refining, finished product oil is obtained by filtering. The specific process is as follows: in a reactor, raw material oil and furfural are proportionally added, after full contact reaction, an oil product I is obtained by separation, after the first carclazyte refining of the oil product I, an oil product II is obtained by filtering, the oil product II is adsorbed and refined by the adsorbent to obtain an oil product III, and after the secondary carclazyte refining of the oil product III, the finished product oil is obtained by filtering. The process can make silicon content of the finished product oil less than 2ppm and foaming tendency less than 50ml, so that excellent foam properties are shown.
Description
Technical field
The present invention relates to a kind of used oil refining process, particularly relate to a kind of technique improving foam tendency in used oil refining process.
Background technology
Used oil refining technology has developed more and more ripe at present, and the recovery of used oil not only can protection of the environment, can also save and recycle these valuable sources greatly.But, in existing used oil refining process, the technique of some routines is as distillation cutting, the lubricant base of furfural treatment and clay-filtered generation, although majority parameters all meets the demands, but at some high-speed gears, in large volume pumping machine oil rare earth, require that base oil must have fabulous foam characteristic, when namely requiring that foam tendency controls in the scope of < 50ml, owing to containing a large amount of additives in used oil, its silicone content is higher, and be limited in existing used oil refining process, crude oil after used oil distillation cutting is only through furfural and clay-filtered, its silicone content is still up to 150-300ppm, foam tendency is still at more than 350ml, the requirement of foam tendency < 50ml cannot be reached.And base oil foam will be made to be inclined to < 50ml, its silicone content must control to <5ppm.
Summary of the invention
The object of the invention is for the above-mentioned problems in the prior art, propose one and can make base oil silicone content <2ppm, the technique of foam tendency in the improvement used oil refining process of foam tendency < 50ml.
Object of the present invention realizes by following technical proposal: a kind of technique improving the tendency of foam in used oil refining process, and it is clay-filtered that described technique mainly comprises furfural treatment, once clay-filtered, refining with adsorbents and secondary; Described refining with adsorbents and secondary clay-filtered be primary purification is filtered the oil product that obtains to carry out clay-filtered after adsorbent is refining again, refined rear filtration and obtained processed oil.
In used oil refining process of the present invention, in original furfural treatment and clay-treated basis, add refining with adsorbents and secondary is clay-filtered.Make through first time clay-filtered after silicone content still within the scope of 150-300ppm, foam tendency still more than 350ml oil product through refining with adsorbents and secondary clay-filtered after, the silicone content <2ppm of oil product, foam is made to be inclined to < 50ml, base oil is made to have fabulous foam characteristic, meet such as some high-speed gears, in large volume pumping oiling system, high environment for use is required to base oil foam characteristic.
A kind ofly to improve in the technique of foam tendency in used oil refining process above-mentioned, described technique mainly comprises the following steps:
Furfural treatment: in reactor, in mass ratio for 1:(2-5) to add temperature be stock oil and the temperature of 60-70 DEG C is the furfural of 90-100 DEG C, carry out abundant contact reacts 2-3h, separation obtains oil product I;
Once clay-filtered: the oil product I above-mentioned separation obtained carries out once clay-filtered, has refined rear filtration and has obtained oil product II;
Refining with adsorbents: the oil product II above-mentioned filtration obtained obtains oil product III after adsorbent is refining;
Secondary is clay-filtered: it is clay-filtered oil product III obtained above to be carried out secondary, has refined rear filtration and has obtained processed oil.
A kind ofly to improve in the technique of foam tendency in used oil refining process above-mentioned, described once clay-filtered middle carclazyte consumption is the 2-4% of the quality of oil product I, and extraction temperature is 130-140 DEG C, and the time is 100-150min.The present invention is once clay-filtered is in order to the colloid in adsorpting lubrication oil, impurity and micro-moisture.After once clay-filtered, oil product colourity is more as clear as crystal, and every physical and chemical index is better.
A kind ofly to improve in the technique of foam tendency in used oil refining process above-mentioned, the clay-filtered middle carclazyte consumption of described secondary is the 1-3% of the quality of oil product III, and extraction temperature is 130-140 DEG C, and the time is 50-80min.The present invention by secondary clay-filtered can further reactive adsorption element silicon be correlated with impurity.
A kind ofly improve in the technique of foam tendency in used oil refining process above-mentioned, decolorizing ability > 150, granularity > 200 order of described carclazyte, free acid < 0.2.The selection of the decolorizing ability of carclazyte of the present invention can guarantee that deimpurity effect is gone in decolouring, and the selection of granularity is then in order to controlled filter speed, and controls to be the acid number index in order to not affect oil product on the free acid of carclazyte.
A kind ofly to improve in the technique of foam tendency in used oil refining process above-mentioned, in described refining with adsorbents, sorbent material is the one in gac, atlapulgite, diatomite, silica gel, molecular sieve.It is colloid class mechanical impurity in order to adsorpting lubrication oil that the present invention increases refining with adsorbents one, and two is to adsorb the relevant component of element silicon.
A kind ofly improve in the technique of foam tendency in used oil refining process above-mentioned, described stock oil is the crude oil of used oil after distillation cutting.
A kind ofly to improve in the technique of foam tendency in used oil refining process above-mentioned, described crude oil is 30-35mm 40 DEG C of kinematic viscosity
2/ s, acid number <0.5mgKOH/g, silicone content >150ppm.
A kind ofly improve in the technique of foam tendency in used oil refining process above-mentioned, the clay-filtered rear employing flame filter press of described once clay-filtered and secondary filters.Flame filter press filtration area is large, and flow is large, and except adapted motor, all adopt high-quality corrosion-resistant stainless steel material to make, work-ing life is of a specified duration.And the airtight filtration of flame filter press application of pressure, filtrate loss is few, and filter quality is good, and efficiency is high.
Due in used oil containing a large amount of additive, thus cause silicone content in used oil higher, and silicone content is important factor affect foam characteristic, silicone content is higher, foam is inclined to larger, thus foam characteristic is poorer.Only the crude oil after used oil distillation cutting is carried out furfural treatment and clay-filtered in prior art, silicone content is still up to 150-300ppm, and only have when silicone content controls to < 5ppm, foam tendency just can reach below 50ml, just can obtain the good base oil of foam characteristic.Therefore, the present invention by the crude oil raw material of used oil after distillation cutting through furfural treatment and once clay-filtered after, then carry out refining with adsorbents and secondary clay-filtered.Refining with adsorbents process is equivalent to a tower, and filler is sorbent material, when oil product is from sorbent material filler back warp mistake, completes adsorption process.And then carry out once clay-filtered after, filter oil product its silicone content < 2ppm after testing of obtaining, foam tendency < 50ml, reaches about 30ml, thus has fabulous foam characteristic.
Compared with prior art, the present invention has the following advantages:
1. the present invention furfural treatment and clay-filtered after carry out refining with adsorbents and secondary clay-filtered, make the base oil silicone content < 2ppm obtained, foam tendency < 50ml, base oil has fabulous foam characteristic.
2. the present invention improves the technique step that introducing is not complicated of foam tendency in used oil refining process and special reagent, and preparation technology is simple, easy, is beneficial to and realizes industrialization, and economic benefit is given prominence to.
Embodiment
Be below specific embodiments of the invention, technical scheme of the present invention is further described, but the present invention is not limited to these embodiments.
Embodiment 1:
Be 30mm 40 DEG C of kinematic viscosity by used oil after distillation cutting
2/ s, acid number 0.3mgKOH/g, silicone content is the stock oil of crude oil as the present embodiment of 180ppm.In reactor, for 1:3, to add temperature be the stock oil of 65 DEG C and temperature is the furfural of 95 DEG C in mass ratio, carries out abundant contact reacts 2h, be separated and obtain oil product I.Then be separated the oil product I obtained carries out once clay-filtered at 135 DEG C, and Refining times is 120min, and carclazyte consumption is 3% of the volume of oil product I, and the decolorizing ability of carclazyte is 160, and granularity is 230 orders, and free acid is 0.15.Refine the filtration of rear employing flame filter press and obtain oil product II.Then by filtering oil product II process from activated carbon of sorbent obtained, completing refining with adsorbents, obtaining oil product III.Finally carry out once clay-filtered at 135 DEG C again by the oil product III obtained, Refining times is 60min, and carclazyte consumption is 2% of the volume of oil product III, and decolorizing ability is 160, and granularity is 230 orders, and free acid is 0.15.Refine the filtration of rear employing flame filter press and obtain processed oil.
Embodiment 2:
Be 32mm 40 DEG C of kinematic viscosity by used oil after distillation cutting
2/ s, acid number is 0.3mgKOH/g, and silicone content is the stock oil of crude oil as the present embodiment of 200ppm.In reactor, for 1:3, to add temperature be the stock oil of 65 DEG C and temperature is the furfural of 95 DEG C in mass ratio, carries out abundant contact reacts 2h, be separated and obtain oil product I.Then be separated the oil product I obtained carries out once clay-filtered at 135 DEG C, and Refining times is 120min, and carclazyte consumption is 3% of the volume of oil product I, and the decolorizing ability of carclazyte is 180, and granularity is 250 orders, and free acid is 0.1.Refine the filtration of rear employing flame filter press and obtain oil product II.Then by filtering oil product II process from activated carbon of sorbent obtained, completing refining with adsorbents, obtaining oil product III.Finally carry out once clay-filtered at 135 DEG C again by the oil product III obtained, Refining times is 60min, and carclazyte consumption is 2% of the volume of oil product III, and decolorizing ability is 180, and granularity is 250 orders, and free acid is 0.1.Refine the filtration of rear employing flame filter press and obtain processed oil.
Embodiment 3:
Be 33mm 40 DEG C of kinematic viscosity by used oil after distillation cutting
2/ s, acid number is 0.2mgKOH/g, and silicone content is the stock oil of crude oil as the present embodiment of 235ppm.In reactor, for 1:3, to add temperature be the stock oil of 65 DEG C and temperature is the furfural of 95 DEG C in mass ratio, carries out abundant contact reacts 2h, be separated and obtain oil product I.Then be separated the oil product I obtained carries out once clay-filtered at 135 DEG C, and Refining times is 120min, and carclazyte consumption is 3% of the volume of oil product I, and the decolorizing ability of carclazyte is 200, and granularity is 280 orders, and free acid is 0.1.Refine the filtration of rear employing flame filter press and obtain oil product II.Then by filtering oil product II process from activated carbon of sorbent obtained, completing refining with adsorbents, obtaining oil product III.Finally carry out once clay-filtered at 135 DEG C again by the oil product III obtained, Refining times is 60min, and carclazyte consumption is 2% of the volume of oil product III, and decolorizing ability is 180, and granularity is 250 orders, and free acid is 0.1.Refine the filtration of rear employing flame filter press and obtain processed oil.
Embodiment 4:
Be 35mm 40 DEG C of kinematic viscosity by used oil after distillation cutting
2/ s, acid number is 0.1mgKOH/g, and silicone content is the stock oil of crude oil as the present embodiment of 300ppm.In reactor, for 1:3, to add temperature be the stock oil of 65 DEG C and temperature is the furfural of 95 DEG C in mass ratio, carries out abundant contact reacts 2h, be separated and obtain oil product I.Then be separated the oil product I obtained carries out once clay-filtered at 135 DEG C, and Refining times is 120min, and carclazyte consumption is 3% of the volume of oil product I, and the decolorizing ability of carclazyte is 210, and granularity is 260 orders, and free acid is 0.1.Refine the filtration of rear employing flame filter press and obtain oil product II.Then by filtering oil product II process from activated carbon of sorbent obtained, completing refining with adsorbents, obtaining oil product III.Finally carry out once clay-filtered at 135 DEG C again by the oil product III obtained, Refining times is 60min, and carclazyte consumption is 2% of the volume of oil product III, and decolorizing ability is 220, and granularity is 280 orders, and free acid is 0.15.Refine the filtration of rear employing flame filter press and obtain processed oil.
Comparative example:
Be 33mm 40 DEG C of kinematic viscosity by used oil after distillation cutting
2/ s, acid number is 0.2mgKOH/g, silicone content be the crude oil of 235ppm as stock oil, through conventional furfural treatment and once clay-filtered after obtain oil product.
The processed oil obtained by embodiment of the present invention 1-4 and comparative example carry out silicone content and the test of foam tendency through the oil product that prior art is obtained, and test result is as shown in table 1.
Table 1: embodiment of the present invention 1-4 and comparative example oil testing result
As known from Table 1, only through furfural and once clay-filtered after the silicone content that records far above 5ppm, foam is inclined to also far above 50ml; And the present invention is at furfural with once on clay-treated basis, carry out refining with adsorbents again and secondary clay-filtered, thus make the silicone content < 2ppm that records, foam tendency < 50ml, at about 30ml, obtain fabulous foam characteristic.
The difference of embodiment 4-6 and embodiment 1-3 is only that the temperature of stock oil is 60 DEG C.
The difference of embodiment 7-9 and embodiment 1-3 is only that the temperature of stock oil is 70 DEG C.
The difference of embodiment 10-12 and embodiment 1-3 is only that the temperature of furfural is 90 DEG C.
The difference of embodiment 13-15 and embodiment 1-3 is only that the temperature of furfural is 100 DEG C.
The difference of embodiment 16-18 and embodiment 1-3 is only that the reaction times of stock oil and furfural is 2.5h.
The difference of embodiment 19-21 and embodiment 1-3 is only that the reaction times of stock oil and furfural is 3h.
The difference of embodiment 22-24 and embodiment 1-3 is only that once clay-filtered middle carclazyte consumption is 2% of the volume of oil product I.
The difference of embodiment 25-27 and embodiment 1-3 is only that once clay-filtered middle carclazyte consumption is 4% of the volume of oil product I.
The difference of embodiment 28-30 and embodiment 1-3 is only that once clay-treated extraction temperature is 130 DEG C.
The difference of embodiment 31-33 and embodiment 1-3 is only that once clay-treated extraction temperature is 140 DEG C.
The difference of embodiment 34-36 and embodiment 1-3 is only that once clay-treated Refining times is 100min.
The difference of embodiment 37-39 and embodiment 1-3 is only that once clay-treated Refining times is 130min.
The difference of embodiment 40-42 and embodiment 1-3 is only that once clay-treated Refining times is 150min.
The difference of embodiment 43-45 and embodiment 1-3 is only that the clay-filtered middle carclazyte consumption of secondary is 1% of the volume of oil product III.
The difference of embodiment 46-48 and embodiment 1-3 is only that the clay-filtered middle carclazyte consumption of secondary is 3% of the volume of oil product III.
The difference of embodiment 49-51 and embodiment 1-3 is only that the clay-treated extraction temperature of secondary is 130 DEG C.
The difference of embodiment 52-54 and embodiment 1-3 is only that the clay-treated extraction temperature of secondary is 140 DEG C.
The difference of embodiment 55-57 and embodiment 1-3 is only that the clay-treated Refining times of secondary is 50min.
The difference of embodiment 58-60 and embodiment 1-3 is only that the clay-treated Refining times of secondary is 70min.
The difference of embodiment 61-63 and embodiment 1-3 is only that the clay-treated Refining times of secondary is 80min.
The difference of embodiment 64-66 and embodiment 1-3 is only that in refining with adsorbents, sorbent material is atlapulgite.
The difference of embodiment 67-69 and embodiment 1-3 is only that in refining with adsorbents, sorbent material is diatomite.
The difference of embodiment 70-72 and embodiment 1-3 is only that in refining with adsorbents, sorbent material is silica gel.
The difference of embodiment 73-75 and embodiment 1-3 is only that in refining with adsorbents, sorbent material is molecular sieve.
The difference of embodiment 76-78 and embodiment 1-3 is only that the mass ratio of stock oil and furfural is 1:2.
The difference of embodiment 79-81 and embodiment 1-3 is only that the mass ratio of stock oil and furfural is 1:4.
The difference of embodiment 82-84 and embodiment 1-3 is only that the mass ratio of stock oil and furfural is 1:5.
In view of the present invention program's embodiment is numerous, each embodiment experimental data is huge numerous, be not suitable for particularize herein to illustrate, but the content of the required checking of each embodiment is all close with the final conclusion obtained, so do not illustrate one by one the detected result of each embodiment herein.
Specific embodiment described herein is only to the explanation for example of the present invention's spirit.Those skilled in the art can make various amendment or supplement or adopt similar mode to substitute to described specific embodiment, but can't depart from spirit of the present invention or surmount the scope that appended claims defines.
Although made a detailed description the present invention and quoted some specific embodiments as proof, to those skilled in the art, only otherwise it is obvious for leaving that the spirit and scope of the present invention can make various changes or revise.
Claims (9)
1. improve a technique for the tendency of foam in used oil refining process, it is characterized in that, it is clay-filtered that described technique mainly comprises furfural treatment, once clay-filtered, refining with adsorbents and secondary; Described refining with adsorbents and secondary clay-filtered be primary purification is filtered the oil product that obtains to carry out clay-filtered after adsorbent is refining again, refined rear filtration and obtained processed oil.
2. a kind of technique improving foam tendency in used oil refining process according to claim 1, it is characterized in that, described technique mainly comprises the following steps:
Furfural treatment: in reactor, in mass ratio for 1:(2-5) to add temperature be stock oil and the temperature of 60-70 DEG C is the furfural of 90-100 DEG C, carry out abundant contact reacts 2-3h, separation obtains oil product I;
Once clay-filtered: the oil product I above-mentioned separation obtained carries out once clay-filtered, has refined rear filtration and has obtained oil product II;
Refining with adsorbents: the oil product II above-mentioned filtration obtained obtains oil product III after adsorbent is refining;
Secondary is clay-filtered: it is clay-filtered oil product III obtained above to be carried out secondary, has refined rear filtration and has obtained processed oil.
3. a kind of technique improving foam tendency in used oil refining process according to claim 2, it is characterized in that, described once clay-filtered middle carclazyte consumption is the 2-4% of the quality of oil product I, and extraction temperature is 130-140 DEG C, and the time is 100-150min.
4. a kind of technique improving foam tendency in used oil refining process according to claim 2, it is characterized in that, the clay-filtered middle carclazyte consumption of described secondary is the 1-3% of the quality of oil product III, and extraction temperature is 130-140 DEG C, and the time is 50-80min.
5. a kind of technique improving foam tendency in used oil refining process according to Claims 2 or 3 or 4, it is characterized in that, decolorizing ability > 150, granularity > 200 order of described carclazyte, free acid < 0.2.
6. a kind of technique improving foam tendency in used oil refining process according to claim 2, it is characterized in that, in described refining with adsorbents, sorbent material is the one in gac, atlapulgite, diatomite, silica gel, molecular sieve.
7. a kind of technique improving foam tendency in used oil refining process according to claim 2, is characterized in that, described stock oil is the crude oil of used oil after distillation cutting.
8. a kind of technique improving foam tendency in used oil refining process according to claim 7, it is characterized in that, described crude oil is 30-35mm 40 DEG C of kinematic viscosity
2/ s, acid number <0.5mgKOH/g, silicone content >150ppm.
9. a kind of technique improving foam tendency in used oil refining process according to claim 2, is characterized in that, the clay-filtered rear employing flame filter press of described once clay-filtered and secondary filters.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109762593A (en) * | 2019-02-19 | 2019-05-17 | 安徽国孚凤凰科技有限公司 | A method of improving waste lubricating oil solvent refining Reclaimed Base Oil oxidation stability |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4073719A (en) * | 1977-04-26 | 1978-02-14 | The United States Of America As Represented By The United States Department Of Energy | Process for preparing lubricating oil from used waste lubricating oil |
| CN102766479A (en) * | 2012-07-24 | 2012-11-07 | 中国石油化工股份有限公司 | Method for decolorizing and refining lubricating oil basic oil |
-
2014
- 2014-11-25 CN CN201410686439.4A patent/CN104531209B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4073719A (en) * | 1977-04-26 | 1978-02-14 | The United States Of America As Represented By The United States Department Of Energy | Process for preparing lubricating oil from used waste lubricating oil |
| CN102766479A (en) * | 2012-07-24 | 2012-11-07 | 中国石油化工股份有限公司 | Method for decolorizing and refining lubricating oil basic oil |
Non-Patent Citations (1)
| Title |
|---|
| 徐先盛: "我国废润滑油再生加工工艺、策略及XXS废油再生新工艺研究", 《润滑油》, no. 4, 31 December 1995 (1995-12-31) * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109762593A (en) * | 2019-02-19 | 2019-05-17 | 安徽国孚凤凰科技有限公司 | A method of improving waste lubricating oil solvent refining Reclaimed Base Oil oxidation stability |
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