CN103160319B - Method for improving aromatic hydrocarbon content of petroleum fraction - Google Patents
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- CN103160319B CN103160319B CN201110419845.0A CN201110419845A CN103160319B CN 103160319 B CN103160319 B CN 103160319B CN 201110419845 A CN201110419845 A CN 201110419845A CN 103160319 B CN103160319 B CN 103160319B
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- 238000000034 method Methods 0.000 title claims abstract description 73
- 239000003208 petroleum Substances 0.000 title claims abstract description 19
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title abstract description 5
- 239000003921 oil Substances 0.000 claims abstract description 49
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 33
- 239000002994 raw material Substances 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 239000010779 crude oil Substances 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 12
- 239000001257 hydrogen Substances 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000002184 metal Substances 0.000 claims abstract description 4
- 229910052751 metal Inorganic materials 0.000 claims abstract description 4
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 3
- 229910052721 tungsten Inorganic materials 0.000 claims abstract description 3
- 238000005194 fractionation Methods 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 2
- 238000005336 cracking Methods 0.000 claims 3
- 125000003118 aryl group Chemical group 0.000 abstract description 11
- 238000007670 refining Methods 0.000 abstract description 5
- 150000001336 alkenes Chemical class 0.000 abstract description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 2
- 238000004227 thermal cracking Methods 0.000 abstract 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract 1
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 239000007788 liquid Substances 0.000 abstract 1
- 229910052750 molybdenum Inorganic materials 0.000 abstract 1
- 238000004073 vulcanization Methods 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 31
- 238000005520 cutting process Methods 0.000 description 21
- 230000000052 comparative effect Effects 0.000 description 13
- 229920001971 elastomer Polymers 0.000 description 12
- 239000002904 solvent Substances 0.000 description 7
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000006837 decompression Effects 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- 230000000171 quenching effect Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 208000005623 Carcinogenesis Diseases 0.000 description 2
- 230000036952 cancer formation Effects 0.000 description 2
- 231100000504 carcinogenesis Toxicity 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 231100000252 nontoxic Toxicity 0.000 description 2
- 230000003000 nontoxic effect Effects 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000010692 aromatic oil Substances 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for improving aromatic hydrocarbon content of petroleum fraction. The method is as below: conducting a thermal cracking reaction on raw materials comprising crude oil, atmospheric residual oil, residual oil and a 360-520 DEG C vacuum fraction, and fractionating to obtain a 360-520 DEG C fraction; and hydrofining the fraction to obtain a distillate oil. The thermal cracking reaction requires the following conditions: entrance temperature of 360 DEG C-480 DEG C, and pressure of 0.1-2.0MPa; the hydrofining reaction requires the following conditions: temperature of 250 DEG C-400 DEG C, hydrogen partial pressure of 2-20MPa, liquid hourly space velocity of 0.2-2.0 h, volumetric ratio of hydrogen to oil of 300:1-1500:1; and active metal components in a catalyst comprise one or more from W, Ni, Co and Mo, or a combination thereof, and a carrier Al2O3 is subjected to vulcanization treatment before usage. The fraction subjected to hydrogenation refining removal, olefin saturation and aromatic hydrogenation hydrogenation; and the oil fraction produced from hydrogenation is fractionated to obtain a 360-520 DEG C fraction with aromatic content increased by 1%-30%.
Description
Technical field
The present invention relates to utilize thermocracking process to improve the method for petroleum fractions aromaticity content.
Background technology
Oil is mainly by alkane, naphthenic hydrocarbon, three kinds of hydrocarbon compositions of aromatic hydrocarbon, three kinds of shared ratios of hydro carbons of crude oil that different areas and Different Strata are produced are also not quite similar, be divided into several crude oil such as paraffinic base, cycloalkyl, aromatic base according to three kinds of hydro carbons proportion differences, in petroleum refining process, based on crude kind is determined optimum processing route and scheme conventionally.Along with widening of petroleum products range of application, also increasing to the oil product demand of high aromaticity content, the oil product of high aromaticity content mainly contains two sources, and one is the petroleum fractions that aromatic base crude oil is produced, and another kind is the extraction oil that solvent treatment is produced.At present, aromatic base crude oil proportion is less, and along with the development of oil Refining Technologies, solvent refining unit is also fewer and feweri, causes the oil product source of high aromaticity content fewer and feweri, cannot meet the need of market.
CN1570037A discloses a kind of production technique of high aromatic rubber oil, what relate to is the production technique of the black rubber oil that uses in rubber industry, adopt the catalytic cracking turning oil of slag-mixing amount 20% as raw material, the Extract of lube oil furfural refining unit carries out the method for the high aromatic oil that extracting obtains as solvent.CN 101386687A discloses a kind of aromatic rubber oil and production method thereof, that to subtract three distillates be that raw material carries out solvent extraction and obtains primary purification oil and once extract oil out, carry out secondary solvent extracting and obtain secondary fine liquefaction and secondary and extract oil out once extracting oil out, secondary fine liquefaction is through the clay-filtered aromatic rubber oil that obtains, the standby rubber oil aromaticity content of this legal system is high, polycyclic aromatic hydrocarbon content is less than 3%, and nontoxic without carcinogenesis.CN101597513 discloses a kind of environment-friendly rubber oil and preparation method thereof, that to subtract three distillates be that raw material carries out solvent extraction and obtains primary purification oil and once extract oil out, primary purification oil is carried out to secondary that secondary solvent extracting obtains to be extracted oil out and is environment-friendly rubber oil, the environment-friendly rubber oil aromaticity content of this invention is high, environmental protection, nontoxic, without carcinogenesis, can be used as the substitute of existing aromatic hydrocarbon oil, there is very bright application prospect; CN123945 discloses a kind of taking light base oil as raw material, adds the method for plasticising solubilizing agent production unsaturated rubber extending oil.USP6,248,929 provide a kind of method of producing high aromatic rubber oil taking dimethyl sulfoxide (DMSO) as solvent.
The high aromatic rubber oil of above-mentioned production mainly adopts solvent extraction process for purification to prepare, and does not relate to other processing method and improves petroleum fractions aromaticity content.
Summary of the invention
The object of this invention is to provide a kind of method that adopts thermally splitting-hydrofining combination process to improve petroleum fractions aromaticity content.This invention can improve aromaticity content 1%～30% on former distillate basis.
The present invention, taking crude oil, long residuum, vacuum residuum and vacuum distillate as raw material, enters in the adiabatic reactor that disperses inner member or sky after being heated to suitable temperature of reaction, and reacted product obtains 360 DEG C～520 DEG C cuts through cooling, fractionation; This cut removes the heteroatomss such as S, N, O through hydrofining, and carries out olefin saturated and aromatic hydrogenation, obtains the more former cut of distillate aromaticity content and improves 1%～30%.
Specifically, technical scheme provided by the invention is: taking 500 DEG C of residual oil of long residuum, > of 350 DEG C of crude oil, >, 360 DEG C～520 DEG C reduced pressure distillates as raw material, be heated to after 360～480 DEG C and enter in the adiabatic reactor that disperses inner member or sky through process furnace, disperseing inner member is bubble deck, valve tray, traverse baffle or filler, control raw material 10～180 minutes residence time in reactor, pressure 0.1～2.0MPa; Reactor reactant flow is out cooling through quenching oil, and quenching oil is that cooling rear thermally splitting generates oil, is cooled to 300～380 DEG C; Thermally splitting generates oil and obtains 360～520 DEG C of cuts through fractionation cutting; 360～520 DEG C of cuts and hydrogen mixing post-heating to 250 DEG C～400 DEG C are entered to hydrofining reaction bed, and controlling reaction bed temperature is 250 DEG C～400 DEG C, and hydrogen dividing potential drop is 2.0～20MPa, and volume space velocity is 0.2～2.0h
-1, hydrogen to oil volume ratio 300: 1～1500: 1, hydrogenated oil obtains 360～520 DEG C of cut aromaticity content values through fractionation and improves 1%～30%.
Or rather, technical scheme of the present invention is: taking any cut between 360 DEG C～520 DEG C of 500 DEG C of residual oil of long residuum, >, the reduced pressure distillates of 350 DEG C of crude oil, > as raw material, be heated to after 390～450 DEG C and enter in the adiabatic reactor that disperses inner member or sky through process furnace, inner member is bubble deck, valve tray, traverse baffle or filler, control raw material 20～90 minutes residence time in reactor, pressure 0.1～1.6MPa; Reactor reactant flow is out cooling through quenching oil, and quenching oil is that cooled thermally splitting generates oil, is cooled to 300～360 DEG C; Thermally splitting generates oil and obtains 360～520 DEG C of cuts through fractionation cutting; 360～520 DEG C of cuts and hydrogen mixing post-heating to 280 DEG C～350 DEG C are entered to hydrofining reaction bed, and controlling reaction bed temperature is 290 DEG C～360 DEG C, and hydrogen dividing potential drop is 5.0～16MPa, and volume space velocity is 0.5～1.0h
-1, hydrogen to oil volume ratio 300: 1～800: 1, hydrogenated oil obtains 360～520 DEG C of cut aromaticity contents through fractionation and improves 1%～30%.
The present invention uses catalyst for refining at hydrofining reaction bed, and the active metal component of catalyzer is W, Ni, and Co, one or two or more kinds combination in Mo, accounts for 10～40% of catalyst weight in oxide compound active metal component content, and carrier is Al
2o
3before use, carry out sulfidizing.
The present invention utilizes thermally splitting-hydrofining combination process to improve the aromaticity content of petroleum fractions, the method can be widened high aromaticity content petroleum fractions source, can improve equal distillate aromaticity content value 1%～30%, the aromaticity content that obtains petroleum fractions can reach 5%-35%.
Embodiment
Further set forth technical solution of the present invention and effect below in conjunction with embodiment.
Petroleum fractions arene content determination adopts ASTM D2140 assay method.
Embodiment 1:
Taking crude oil A as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, 360～520 DEG C of cuts during this cut obtains through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 2: taking crude oil B as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 3:
Taking crude oil C as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 4: taking long residuum D as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 5:
Taking long residuum E as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 6:
Taking long residuum F as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 7:
Taking vacuum residuum G as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 8: taking vacuum residuum H as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 9:
Taking vacuum residuum I as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 10: taking 360 DEG C-520 DEG C decompression petroleum fractions J as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 11:
Taking 360 DEG C～520 DEG C decompression petroleum fractions K as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 12:
Taking 360 DEG C～520 DEG C decompression petroleum fractions L as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Embodiment 13:
Taking 360 DEG C～520 DEG C decompression petroleum fractions M as raw material, character, in table 1, is carried out thermocracking process, and thermocracking process operational condition is in table 3.Obtain 360～520 DEG C of cuts through cut cutting, this cut obtains 360～520 DEG C of cuts through hydrogenation production technique.Each production technique operating parameters is in table 4.Hydrogenation catalyst character is in table 5, and each cut aromaticity content value is in table 6.
Comparative example 1:
Taking crude oil A as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, and each cut aromaticity content value is in table 2.Embodiment 1 is compared with comparative example 1: 360-400 DEG C of cut aromaticity content increased by 8%, 400-450 DEG C of cut aromaticity content and increased by 8%, 450-520 DEG C of cut aromaticity content and increased by 8%.
Comparative example 2:
Taking crude oil B as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, and each cut aromaticity content value is in table 2.Embodiment 2 is compared with comparative example 2: 360-400 DEG C of cut aromaticity content increased by 1%, 400-450 DEG C of cut aromaticity content and increased by 5%, 450-520 DEG C of cut aromaticity content and increased by 6%.
Comparative example 3:
Taking crude oil C as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, and each cut aromaticity content value is in table 2.Embodiment 3 is compared with comparative example 3: 360-400 DEG C of cut aromaticity content increased by 5%, 400-450 DEG C of cut aromaticity content and increased by 3%, 450-520 DEG C of cut aromaticity content and increased by 2%.
Comparative example 4:
Taking long residuum D as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, and each cut aromaticity content value is in table 2.Embodiment 4 is compared with comparative example 4: 360-400 DEG C of cut aromaticity content increased by 27%, 400-450 DEG C of cut aromaticity content and increased by 30%, 450-520 DEG C of cut aromaticity content and increased by 16%.
Comparative example 5: taking long residuum E as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, each cut aromaticity content value is in table 2.Embodiment 5 is compared with comparative example 5: 360-400 DEG C of cut aromaticity content increased by 7%, 400-450 DEG C of cut aromaticity content and increased by 10%, 450-520 DEG C of cut aromaticity content and increased by 17%.
Comparative example 6:
Taking long residuum F as raw material, character, in table 1, is carried out cut cutting, obtains 360～520 DEG C of cuts, and each cut aromaticity content value is in table 2.Embodiment 6 is compared with comparative example 6: 360-400 DEG C of cut aromaticity content increased by 12%, 400-450 DEG C of cut aromaticity content and increased by 10%, 450-520 DEG C of cut aromaticity content and increased by 10%.
The analysis of table 1 feedstock property
Table 2 comparative example petroleum fractions aromaticity content value
Table 3 thermally splitting operating parameters and property analysis
Table 4 hydrofining operational condition and property analysis
The analysis of table 5 catalyst property
Table 6 embodiment petroleum fractions aromaticity content is analyzed
Claims (2)
1. one kind is improved the method for petroleum fractions aromaticity content, it is characterized in that: taking any cut between 360 DEG C～520 DEG C of long residuum, >500 DEG C residual oil, the reduced pressure distillates of crude oil, >350 DEG C as raw material, through heat cracking reaction, fractionation obtains 360～520 DEG C of cuts; This cut obtains distillate through hydrofining;
The processing condition of heat cracking reaction are: temperature in is 360 DEG C～480 DEG C, 10～180 minutes residence time, pressure 0.1～2.0MPa;
Entering the processing condition that the first hydrogenation reaction bed carries out hydrofining reaction under Hydrobon catalyst effect is: temperature is 250 DEG C～400 DEG C, and hydrogen dividing potential drop is 2.0～20MPa, and volume space velocity is 0.2～2.0h
-1, hydrogen to oil volume ratio 300:1～1500:1;
Hydrofining bed uses Hydrobon catalyst, and the active metal component of catalyzer is W, Ni, and Co, a kind of or its combination in Mo, accounts for 10%～40% of catalyst weight in oxide compound active metallic content, and carrier is Al
2o
3, before use, carry out sulfidizing.
2. according to the method for raising petroleum fractions aromaticity content claimed in claim 1, it is characterized in that: entering the processing condition of carrying out heat cracking reaction in an adiabatic reactor is: temperature in is 390 DEG C～450 DEG C, 20～90 minutes residence time, pressure 0.1～1.6MPa;
Entering the processing condition that the first hydrogenation reaction bed carries out hydrofining reaction under Hydrobon catalyst effect is: temperature is 290 DEG C～360 DEG C, and hydrogen dividing potential drop is 5～16MPa, and volume space velocity is 0.5～1.0h
-1, hydrogen to oil volume ratio 300:1～800:1.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4619757A (en) * | 1982-08-31 | 1986-10-28 | Linde Aktiengesellschaft | Two stage hydrotreating pretreatment in production of olefins from heavy hydrocarbons |
| US5167847A (en) * | 1990-05-21 | 1992-12-01 | Exxon Research And Engineering Company | Process for producing transformer oil from a hydrocracked stock |
| CN101646750A (en) * | 2007-04-19 | 2010-02-10 | 昭和电工株式会社 | Hydrogenation method and petrochemical process |
-
2011
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4619757A (en) * | 1982-08-31 | 1986-10-28 | Linde Aktiengesellschaft | Two stage hydrotreating pretreatment in production of olefins from heavy hydrocarbons |
| US5167847A (en) * | 1990-05-21 | 1992-12-01 | Exxon Research And Engineering Company | Process for producing transformer oil from a hydrocracked stock |
| CN101646750A (en) * | 2007-04-19 | 2010-02-10 | 昭和电工株式会社 | Hydrogenation method and petrochemical process |
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Effective date of registration: 20180718 Address after: 100007 Dongzhimen North Street, Dongcheng District, Dongcheng District, Beijing Co-patentee after: CNPC KARAMAY PETROCHEMICAL CO.,LTD. Patentee after: PetroChina Company Limited Address before: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Patentee before: PetroChina Company Limited |
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