CN1990833A - Production method for extra high voltage transformer oil - Google Patents
Production method for extra high voltage transformer oil Download PDFInfo
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- CN1990833A CN1990833A CN 200510132293 CN200510132293A CN1990833A CN 1990833 A CN1990833 A CN 1990833A CN 200510132293 CN200510132293 CN 200510132293 CN 200510132293 A CN200510132293 A CN 200510132293A CN 1990833 A CN1990833 A CN 1990833A
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Abstract
The invention provides a method for preparing super- voltage transformer oil. It comprises following steps: making naphthenic base oil contact with hydrogenation treatment catalyst and hydrogenation refining catalyst in sequence under hydrogenation process condition; said hydrogenation treatment catalyst contains a thermal- resistant inorganic oxidant carrier and cobalt and/ or nickel, molybdenum and/ or tungsten and fluoride or phosphorus that loaded on said carrier, the total airspeed of said naphthenic base oil is 0.2- 1 h-1, and the relative airspeed of hydrogenation treatment catalyst is 0.3- 1.2 h-1, the relative airspeed of hydrogenation refining catalyst is 0.3- 2h-1.
Description
Technical field
The present invention relates to a kind of production method of transformer oil, more specifically to a kind of production method of ultrahigh voltage transformer oil.
Background technology
Transformer oil is a kind of liquid insulating heat-conduction material of being produced by mineral oil, and its performance is relevant with the composition of institute's hydrocarbonaceous.For example, poor, the easy liberation of hydrogen of straight-chain paraffin low-temperature fluidity is the undesirable components in the transformer oil; The anti-gassing performance of aromatic hydrocarbons is good, but the polycyclic aromatic hydrocarbons oxidation stability is poor, and easy oxidation discoloration and generation precipitation also must remove or reduce its content usually in the course of processing.
In the prior art, can adopt the kinds of processes method to produce transformer oil.For example, and employing hydrofining-furfural treatment-clay-filtered processing method production transformer oil (Li Huixin etc. utilize huge port sheep three wooden low-sulfur naphthenic base crudes to produce the 45# transformer oil, lubricating oil, and the 18th the 4th phase of volume, 2003,60-62); CN1174225 discloses a kind of transformer oil and method for making thereof, and this method is that raw material is produced transformer oil with the catalytic pyrolysis light oil that is rich in aromatic hydrocarbons.The alkylaromatic hydrocarbon quantity that this transformer oil contains is far longer than the transformer oil that traditional technology makes, and has good electrical property, and the outward appearance water-white is transparent.But, can't make the ultrahigh voltage transformer oil that can meet the demands by these methods.
It is raw material with the atmospheric distillate that people such as Guo Huai disclose a kind of, adopts alkali cleaning make with extra care-to sneak into the extraction oil of an amount of furfural solvent treatment by-product-hydrofining technology and produces the ultrahigh voltage transformer oil method (refining of petroleum and chemical industry, the 30th rolled up for the 2nd phase, 56-57).But the alkali cleaning in this method not only can bring a large amount of environmental problems, also can reduce the yield of purpose product simultaneously greatly.
Summary of the invention
The objective of the invention is on the basis of existing technology, a kind of method of new production ultrahigh voltage transformer oil is provided.
Method provided by the invention comprises: under the hydrofining technology condition, the naphthene base crude oil charging is contacted with a kind of Hydrobon catalyst with a kind of hydrotreating catalyst successively, described hydrotreating catalyst contains a kind of heat-resistant inorganic oxide carrier and the cobalt and/or nickel, molybdenum and/or tungsten and fluorine or the phosphorus that load on this carrier, Hydrobon catalyst contains a kind of heat-resistant inorganic oxide carrier and the cobalt and/or nickel and molybdenum and/or the tungsten that load on this carrier, wherein, total air speed of described naphthene base crude oil charging is 0.2-1h
-1, the consumption of hydrotreating catalyst Hydrobon catalyst, making the naphthene base crude oil charging is 0.3-1.2h with respect to the hydrotreating catalyst air speed
-1, be 0.3-2h with respect to the Hydrobon catalyst air speed
-1
Compare with existing method, the invention provides method and not only can directly be used for producing ultrahigh voltage transformer oil, and product yield obviously improves.For example process same materials oil, the invention provides method in employing and produce the product ultrahigh voltage transformer oil, its yield can reach 75.2 weight %; And adopting existing method to produce ultrahigh voltage transformer oil, its yield only is 68.5 weight %.
Embodiment
According to method provided by the invention, described naphthene base crude oil be class feature factor K value＜11.5 crude oil (Hou Xianglin, Chinese oil Refining Technologies, Sinopec press, 1991,8-9).Described naphthene base crude oil charging is selected from the atmospheric distillate of naphthenic base crude and in the vacuum distillate one or more, and preferred total aromaticity content is the naphthene base crude oil of 16-45%, further is optimized for the naphthene base crude oil that total aromaticity content is 20-40%
According to method provided by the invention, described hydrotreating catalyst and Hydrobon catalyst preferably fill in respectively in two or more reactors.The filling of hydrotreating catalyst and Hydrobon catalyst contacts the stock oil that enters reactor successively with Hydrobon catalyst with hydrotreating catalyst, wherein, total air speed of described naphthene base crude oil charging is preferably 0.3-0.5h
-1, and the air speed that satisfies with respect to hydrotreating catalyst is 0.4-0.7h
-1, be 0.6-1.5h with respect to the air speed of Hydrobon catalyst
-1
According to method provided by the invention, described hydrotreating catalyst is the habitual hydrotreating catalyst in this area, cobalt wherein and/or nickel, molybdenum and/or tungsten and fluorine or phosphorus content are conventional content, in oxide compound and with the catalyzer is benchmark, the cobalt and/or the nickel that preferably contain 1-8 weight %, molybdenum and/or the tungsten of 10-35 weight %, in element, fluorine or the phosphorus of 1-6 weight %.
According to method provided by the invention, can also also have molecular sieve in the described hydrotreating catalyst, described molecular screening one or more in zeolite or non-zeolitic molecular sieves, preferred bore dia is the molecular sieve of 0.6-0.8 nanometer, as be selected among L zeolite, y-type zeolite, X type zeolite, Beta zeolite, mordenite, ZSM-3, ZSM-4, ZSM-18, ZSM-20, the SAPO-5 one or more, Y zeolite more preferably, more preferred Y zeolite through super stabilizing.
According to the invention provides method, it is in common knowledge that described hydrorefined type or composition are similarly this area.For example, CN 1085934A discloses a kind of catalyst for hydrogen refining of paraffin wax, and this catalyzer is made up of magnesium oxide, nickel oxide and Tungsten oxide 99.999 and aluminum oxide; The disclosed a kind of non-precious metal catalyst that loads on aluminum oxide or the silica-alumina carrier of CN 1140748A, this catalyzer contains the nickel of 5-30 weight %, the molybdenum of 1-10 weight %, the silicon oxide of 0-15 weight % and the aluminum oxide of surplus.About details of these catalyzer and preparation method thereof, in relevant patent, disclose in detail, repeat no more herein.
Described heat-resistant inorganic oxide is selected from one or more in the various heat-resistant inorganic oxides that are commonly used for support of the catalyst and/or matrix.For example, one or more in optional self-alumina, silicon oxide, titanium oxide, magnesium oxide, silica-alumina, aluminum oxide-magnesium oxide, silicon oxide-magnesium oxide, silicon oxide-zirconium white, silicon oxide-Thorotrast, silicon oxide-beryllium oxide, silicon oxide-titanium oxide, silicon oxide-zirconium white, oxidation titania-zirconia, silica-alumina-Thorotrast, silica-alumina-titanium oxide, silica-alumina-magnesium oxide, silica-alumina-zirconium white, natural zeolite, the clay.Be preferably aluminum oxide and/or silicon oxide.
According to the ordinary method in this area, described catalyzer in the presence of hydrogen, carried out prevulcanized with sulphur, hydrogen sulfide or sulfur-bearing raw material usually under 140-370 ℃ temperature before using, this prevulcanized can be carried out also can original position vulcanizing in device outside device, is translated into sulfide type.
According to the invention provides method, except that air speed, other reaction conditionss that described naphthene base crude oil charging contacts with a kind of Hydrobon catalyst with a kind of hydrotreating catalyst successively comprise that temperature of reaction, pressure hydrogen to oil volume ratio can be the same or different.Described reaction conditions is the habitual reaction conditions in this area.Usually, preferable reaction temperature is 150 ℃-420 ℃, more preferably 220 ℃-370 ℃, and the hydrogen dividing potential drop is preferably 1-25MPa, 6-16MPa more preferably, and hydrogen to oil volume ratio is preferably 80-2000, more preferably 100-1500.When described hydrotreating catalyst and Hydrobon catalyst fill in two or more different reactor respectively, preferably at the reactor that is filled with hydrotreating catalyst be filled with between the reactor of Hydrobon catalyst and also comprise heat-exchanger rig, described naphthene base crude oil charging is through contacting with hydrotreating catalyst in being filled with the reactor of hydrotreating catalyst, go into to be filled with after the heat exchange in the reactor of Hydrobon catalyst and contact with Hydrobon catalyst, preferable reaction temperature when described naphthene base crude oil charging contacts with hydrotreating catalyst is 150 ℃-420 ℃, more preferably 250 ℃-380 ℃, the hydrogen dividing potential drop is preferably 1-25MPa, 6-20MPa more preferably, hydrogen to oil volume ratio is preferably 80-2000, more preferably 200-1500; Preferable reaction temperature when described naphthene base crude oil charging contacts with Hydrobon catalyst is 150 ℃-420 ℃, more preferably 220 ℃-350 ℃, the hydrogen dividing potential drop is preferably 1-25MPa, 6-20MPa more preferably, hydrogen to oil volume ratio is preferably 80-2000, more preferably 200-1500.
According to method provided by the invention, also comprise one or more separation steps, the described known technology that is separated into this area is as distillation or the isolating method of high-pressure gas-liquid.Described distillation can comprise the operating unit of one or more flash distillations, air distillation and underpressure distillation usually, to finish desirable separation.
Method provided by the invention is a raw material with the naphthene base crude oil, is particularly suitable for producing ultrahigh voltage transformer oil.
The following examples will the present invention will be further described.
Employed hydrotreating catalyst in the embodiment of the invention, Hydrobon Catalyst And Its Preparation Method are as follows:
1. hydrotreating catalyst A
Employed hydrotreating catalyst A in the embodiment of the invention, for what prepare according to the example among the CN 1057021C 6 is auxiliary agent with the fluorine, nickel-tungsten is the catalyzer of active constituent loading on alumina supporter, be benchmark with the catalyzer total amount wherein, in oxide compound, the content of nickel is 2.3 weight %, the content of tungsten is 22 weight %, in element, the content of fluorine is 4 weight %, and all the other are aluminum oxide.
2. hydrogenation catalyst B
Employed Hydrobon catalyst B in the embodiment of the invention, catalyst B is according to the method preparation of CN 1085934A, and wherein nickel oxide content is 3.1 weight %, and tungstic oxide content is 32.5 weight %, and content of magnesia is 1.1 weight %, surplus is an aluminum oxide.
Embodiment 1
The present embodiment explanation the invention provides the effect of method.
Stock oil is the cycloalkyl atmospheric distillate, and its character sees Table 1.300 milliliters of hydrotreating catalyst A and Hydrobon catalyst B are packed into respectively among two fixed bed hydrogenation reactor I and the II for 150 milliliters.At first with catalyst A and B prevulcanized, vulcanized oil is the kerosene that contains dithiocarbonic anhydride 2.0 weight % before the logical stock oil, and cure conditions is: hydrogen dividing potential drop 12 MPas, 370 ℃ of temperature, total air speed 1.0h-1, hydrogen-oil ratio 400, curing time 15 hours.
Switch stock oil after the prevulcanized successively by reactor I and II.Control hydrotreatment reaction zone reaction conditions is: hydrogen dividing potential drop 12 MPas, 340 ℃ of temperature, air speed 0.6h
-1, hydrogen-oil ratio 800: 1; Control hydrofining reaction district reaction conditions is: hydrogen dividing potential drop 12 MPas, 220 ℃ of temperature of reaction, air speed 1.2h
-1, hydrogen-oil ratio 800: 1, total air speed is 0.4h
-1Generating oil through distillation, obtain the transformer oil cut, is benchmark with stock oil, and transformer oil cut yield is 82.6%.Call in 0.3% 2,6 ditertiary butyl p cresol in the transformer oil cut, obtain transformer oil, its character sees Table 1.
Comparative Examples 1
Stock oil is identical with embodiment 1, and hydrotreating catalyst A is packed in the fixed bed hydrogenation reactor for 300 milliliters.Before the logical stock oil at first with the method prevulcanized of catalyst A according to embodiment 1.
Switch stock oil after the prevulcanized.Reaction conditions is: hydrogen dividing potential drop 12 MPas, 340 ℃ of hydrotreatment temperature of reaction, air speed 0.4h
-1, hydrogen-oil ratio 800: 1.Generating oil through distillation, obtain the transformer oil cut, is benchmark with stock oil, and transformer oil cut yield is 80.5%.Call in 0.3% 2,6 ditertiary butyl p cresol in the transformer oil cut, obtain transformer oil, its character sees Table 1.
Table 1
| Stock oil | Embodiment 1 | Comparative Examples 1 | SH0040-91 | Test method | |
| Density (20 ℃)/kgm -3 | 883.9 | 867.6 | 870.3 | ≯895 | GB/T1884 |
| Colourity/number | 2.5 | ＜0.5 | ＜0.5 | ≯1 | GB/T6540 |
| Outward appearance | / | Limpid transparent | Transparent | Transparent nothing precipitation and suspended substance | |
| Kinematic viscosity/mm 2·s -1 100℃ 40℃ | 2.61 12.16 | 2.41 10.01 | 2.43 10.19 | / ≯13 | GB/T265 |
| Pour point/℃ | -45 | -31 | -30 | ≯-22 | GB/T3535 |
| Flash-point (remaining silent)/℃ | 151 | 145 | 146 | ≮140 | GB/T261 |
| Neutralization value/mgKOHg -1 | 4.01 | ＜0.01 | ＜0.01 | ≯0.01 | GB/T4945 |
| Oxidation stability | SH/T0206 | ||||
| Precipitation/% | / | 0.10 | 0.24 | ≯0.2 | |
| Acid number/mgKOHg -1 | / | 0.18 | 0.42 | ≯0.4 | |
| Voltage breakdown/kv | / | 42 | 42 | ≮40 | GB/T507 |
| Dielectric dissipation factor (90 ℃) | / | 0.0015 | 0.004 | ≯0.002 | GB/T5654 |
| Degassing property/μ L/min | / | 4 | 4 | ≯+5 | GB/T11142 |
| Group composition/% stable hydrocarbon aromatic hydrocarbons colloid | 80.9 18.0 1.1 | 87.8 11.8 0.4 | 86.2 12.9 0.9 | / / / | |
| Boiling range/℃ initial boiling point 5% 10% 30% 50% 70% 90% end points of distillation | 272 286 290 300 312 325 346 363 | 267 292 308 322 326 328 332 343 | 265 287 305 313 329 331 334 353 | ASTMD86 |
The result who is listed by table 1 can see, adopts every quality index of the product oil that the method that the invention provides obtains all can reach the specification requirement of SH0040-91 ultrahigh voltage transformer oil; And the product oil that obtains by the reference method, because of oxidation stability (precipitation and acid number) poor, the specification requirement that does not reach the SH0040-91 ultrahigh voltage transformer oil.
Embodiment 2
Stock oil is the cycloalkyl atmospheric distillate, and its character sees Table 3.Hydrotreating catalyst A 375 grams and Hydrobon catalyst B 110 grams are packed into respectively among two placed in-line fixed bed hydrogenation reactor I (300 milliliters) and the II (150 milliliters).Before the logical stock oil at first with catalyst A and B method prevulcanized according to embodiment 1.
Switch stock oil after the prevulcanized successively by reactor I and II.Control hydrotreatment reaction zone reaction conditions is: hydrogen dividing potential drop 12 MPas, 355 ℃ of temperature, air speed 0.4h
-1, hydrogen-oil ratio 800: 1; Control hydrofining reaction district reaction conditions is: hydrogen dividing potential drop 12 MPas, 240 ℃ of temperature of reaction, air speed 0.8h
-1, hydrogen-oil ratio 800: 1, total air speed is 0.27h
-1Generating oil through distillation, obtain the transformer oil cut, is benchmark with stock oil, and transformer oil cut yield is 75.2%.Call in 0.3% 2,6 ditertiary butyl p cresol in the transformer oil cut, obtain transformer oil, its character sees Table 3.
Comparative Examples 2
Stock oil is identical with embodiment 2, and its character sees Table 3.With the alkali cleaning of stock oil process depickling, solvent treatment and the clay-filtered transformer oil that obtains.Processing condition see Table 2, and the transformer oil character that obtains sees Table 3.By table 3 as seen, transformer oil cut yield is 68.5%.
Table 2
| Alkali washing process condition alkali lye add-on/weight % temperature/℃ the settling time/min product yield/weight % | 15.0 80 60 92.0 |
| Temperature in solvent treatment processing condition agent-oil ratio (m/m) tower top temperature/℃ tower/℃ product yield/weight % | 2.5∶1 90 60 76.0 |
| Clay-filtered processing condition carclazyte consumption/weight % treatment temp/℃ product yield/weight % | 3.0 105 98.0 |
| The finished product yield/weight % | 68.5 |
Table 3
| Stock oil | Embodiment 2 | Comparative Examples 2 | SH0040-91 | Test method | |
| Density (20 ℃)/kgm -3 | 906.1 | 867.6 | 870.3 | ≯895 | GB/T1884 |
| Colourity/number | 3.5 | ＜0.5 | 1.0 | ≯1 | GB/T6540 |
| Outward appearance | / | Limpid transparent | / | Transparent nothing precipitation and suspended substance | |
| Kinematic viscosity/mm 2·s -1 100℃ 40℃ | 2.61 12.16 | 2.364 9.682 | 2.61 10.32 | / ≯13 | GB/T265 |
| Pour point/℃ | -38 | -40 | -38 | ≯-22 | GB/T3535 |
| Flash-point (remaining silent)/℃ | 151 | 146 | 149 | ≮140 | GB/T261 |
| Neutralization value/mgKOHg -1 | 4.96 | ＜0.01 | ＜0.01 | ≯0.01 | GB/T4945 |
| Oxidation stability precipitation/% acid number/mgKOHg -1 | / / | 0.10 0.18 | 0.31 0.49 | ≯0.2 ≯0.4 | SH/T0206 |
| Voltage breakdown/kv | / | 46 | 41 | ≮40 | GB/T507 |
| Dielectric dissipation factor (90 ℃) | / | 0.001 | 0.002 | ≯0.002 | GB/T5654 |
| Degassing property/μ L/min | / | 4 | 3 | ≯+5 | GB/T11142 |
| Group composition/% stable hydrocarbon aromatic hydrocarbons colloid | 62.7 34.7 2.6 | 87.8 11.8 0.4 | 84.5 14.7 0.8 | / / / | |
| Boiling range/℃ initial boiling point 5% 10% 30% 50% 70% 90% end points of distillation | 245 287 298 319 327 330 336 347 | 193 218 228 269 285 305 328 326 | 223 255 279 297 302 321 329 334 | / / / / / / / / | ASTMD86 |
The result who is listed by table 3 can see, all can reach the SH0040-91 ultrahigh voltage transformer oil although Comparative Examples 2 can be produced every quality index, and the invention provides method and reduces by 6.7 weight % than its yield, is starkly lower than the present invention.
Claims (11)
1, a kind of production method of ultrahigh voltage transformer oil, this method comprises: under the hydrogenation reaction processing condition, the naphthene base crude oil charging is contacted with a kind of Hydrobon catalyst with a kind of hydrotreating catalyst successively, described hydrotreating catalyst contains a kind of heat-resistant inorganic oxide carrier and loads on the cobalt and/or the nickel of the significant quantity on this carrier, molybdenum and/or tungsten and fluorine or phosphorus, Hydrobon catalyst contains a kind of heat-resistant inorganic oxide carrier and loads on cobalt and/or nickel and the molybdenum and/or the tungsten of the significant quantity on this carrier, wherein, total air speed of described naphthene base crude oil charging is 0.2-1h
-1, the consumption of hydrotreating catalyst and Hydrobon catalyst, making the naphthene base crude oil charging is 0.3-1.2h with respect to the hydrotreating catalyst air speed
-1, be 0.3-2h with respect to the Hydrobon catalyst air speed
-1
2, method according to claim 1 is characterized in that, described hydrotreating catalyst and Hydrobon catalyst fill in respectively in two or more reactors, and total air speed of described naphthene base crude oil charging is 0.3-0.5h
-1, and to satisfy with respect to the hydrotreating catalyst air speed be 0.4-0.7h
-1, be 0.6-1.5h with respect to the Hydrobon catalyst air speed
-1
3, method according to claim 1 and 2 is characterized in that, described hydrotreating catalyst, in oxide compound and with the catalyzer is benchmark, contains cobalt and/or the nickel of 1-8 weight %, molybdenum and/or the tungsten of 10-35 weight %, in element, fluorine or the phosphorus of 1-6 weight %.
4, method according to claim 1 and 2 is characterized in that, described Hydrobon catalyst is a benchmark in oxide compound and with the catalyzer, contains the nickel of 5-30 weight %, the molybdenum of 1-10 weight %.
5, method according to claim 1 is characterized in that, described heat-resistant inorganic oxide is selected from one or more in the various heat-resistant inorganic oxides that are commonly used for support of the catalyst and/or matrix.
6, method according to claim 1 is characterized in that, the temperature of reaction when described naphthene base crude oil charging contacts with hydrotreating catalyst is 150-420 ℃, and the hydrogen dividing potential drop is 1-25MPa, and hydrogen to oil volume ratio is 80-2000.
7, method according to claim 6 is characterized in that, the temperature of reaction when described naphthene base crude oil charging contacts with hydrotreating catalyst is 250-380 ℃, and the hydrogen dividing potential drop is 6-20MPa, and hydrogen to oil volume ratio is 200-1500.
8, method according to claim 1 is characterized in that, the temperature of reaction when described naphthene base crude oil charging contacts with Hydrobon catalyst is 150-420 ℃, and the hydrogen dividing potential drop is 1-25MPa, and hydrogen to oil volume ratio is 80-2000.
9, method according to claim 8 is characterized in that, the temperature of reaction when described naphthene base crude oil charging contacts with Hydrobon catalyst is 220-350 ℃, and the hydrogen dividing potential drop is 6-20MPa, and hydrogen to oil volume ratio is 200-1500.
10, method according to claim 1 is characterized in that, described naphthene base crude oil charging is that total aromaticity content is the naphthene base crude oil of 16-45%.
11, method according to claim 10 is characterized in that, described naphthene base crude oil charging is the naphthene base crude oil of total aromaticity content 18-40%.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102190604A (en) * | 2010-03-03 | 2011-09-21 | 中国石油天然气股份有限公司 | Method for preparing petroleum sulfonate |
| CN102676215A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Method for improving gassing resistance of transformer oil and equipment for producing transformer oil |
| CN101747934B (en) * | 2008-12-08 | 2013-04-24 | 中国石油天然气股份有限公司 | Method for preparing transformer oil anti-gassing additive |
| CN104593059A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Hydrogenation process for FCC recycle oil |
| CN104862006B (en) * | 2015-05-18 | 2016-07-27 | 中国海洋石油总公司 | Anti-evolving-gas additive of transformer oil and preparation method thereof |
| CN109794273A (en) * | 2019-02-20 | 2019-05-24 | 中国海洋石油集团有限公司 | The preparation method of hydrotreating catalyst, preparation method and transformer oil base oil |
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2005
- 2005-12-27 CN CNB200510132293XA patent/CN100537722C/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101747934B (en) * | 2008-12-08 | 2013-04-24 | 中国石油天然气股份有限公司 | Method for preparing transformer oil anti-gassing additive |
| CN102190604A (en) * | 2010-03-03 | 2011-09-21 | 中国石油天然气股份有限公司 | Method for preparing petroleum sulfonate |
| CN102190604B (en) * | 2010-03-03 | 2013-07-31 | 中国石油天然气股份有限公司 | Method for preparing petroleum sulfonate |
| CN102676215A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Method for improving gassing resistance of transformer oil and equipment for producing transformer oil |
| CN102676215B (en) * | 2011-03-08 | 2014-06-04 | 中国石油天然气股份有限公司 | Method for improving gassing resistance of transformer oil and equipment for producing transformer oil |
| CN104593059A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Hydrogenation process for FCC recycle oil |
| CN104593059B (en) * | 2013-11-04 | 2016-05-18 | 中国石油化工股份有限公司 | A kind of FCC recycle oil hydrogenation method |
| CN104862006B (en) * | 2015-05-18 | 2016-07-27 | 中国海洋石油总公司 | Anti-evolving-gas additive of transformer oil and preparation method thereof |
| CN109794273A (en) * | 2019-02-20 | 2019-05-24 | 中国海洋石油集团有限公司 | The preparation method of hydrotreating catalyst, preparation method and transformer oil base oil |
| CN109794273B (en) * | 2019-02-20 | 2021-12-17 | 中国海洋石油集团有限公司 | Hydrotreating catalyst, preparation method thereof and preparation method of transformer oil base oil |
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| CN100537722C (en) | 2009-09-09 |
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