CN1158883A - Hydrocracking process of heavy oil and residual oil in suspension bed - Google Patents
Hydrocracking process of heavy oil and residual oil in suspension bed Download PDFInfo
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Abstract
Active metal components including Mo, Ni, etc. in the mode of aqueous solution are dispersed into heavy oil and residual oil, which is then hydrotreated in suspended bed under the conditions of 10-20 MPa and 380-460 deg.C. Without producing coke, the decompresision residual-oil convertion rate in single process can reach 70%.
Description
The present invention relates to a kind of catalytic hydrocracking method of heavy, residual oil.
Demand because crude oil available on the market becomes heavily day by day to light-end products increases day by day, and the heavy oil lighting has become oil refining worker's main task.The heavy-oil hydrogenation upgrading is one of main method of heavy oil lighting.Its main purpose is metal, the hazardous compounds such as S, N that can slough in a large number in weight, the residual oil, the low boiling component that can make again heavily, slag oil crack becomes high value.
Present more employing fixed-bed reactor of residual hydrogenation, the catalyzer of different purposes are sub-packed in different reactors or the different bed, and residual oil contacts with catalyzer during by bed and carries out hydrogenation reaction.The shortcoming of this technology be processing during poor quality oil bed easily stop up, and the product of device distributes and determined by catalyzer and stock oil basically, is difficult to change with city's field boundary adjust.In order to overcome this shortcoming, adapt to the needs of processing poor residuum, many companies are all in research and development floating bed hydrogenation technology.
U.S. Pat P4637870 has announced industrial phospho-molybdic acid crystal has been dissolved in the technology that is used for suspension bed residual oil hydrogenation in the phosphate aqueous solution.They make catalyst precursor with phospho-molybdic acid-phosphate aqueous solution and hydrocarbon ils earlier, and then are mixed into reactor through dehydration, sulfuration back and resid feed and carry out hydrogenation reaction.This patent emphasizes that the P/Mo atomic ratio of industrial phospho-molybdic acid is 0.08-0.1: 1, and make its total P/Mo atomic ratio reach 0.12-0.45 if add phosphoric acid: can significantly reduce green coke (can reduce to 1.78% from 5.06% in the example) after 1.But for the use in practice, this green coke amount is still earned excessive, and catalyzer before motion device will with the pre-mixing of part hydrocarbon ils, pre-dehydration, this also brings many inconvenience to actually operating.
U.S. Pat P4637871 has announced a similar techniques, and they emphasize that the concentration of molybdenum in the phospho-molybdic acid aqueous solution should be below 5%, if concentration is higher than 5% coking yield and significantly rises.The speed of hydrogenation reaction and the degree of depth depend on the concentration of reactive metal in the reaction system, if use the low phosphorus molybdic acid aqueous solution, make the reactive metal in the reaction system reach enough concentration, certainly will introduce a large amount of moisture content in catalyzer-oil body system.
U.S. Pat P5039392 is the improvement of above-mentioned two patents, and this patent emphasizes that catalyst precursor does vulcanizing agent sulfuration with elementary sulfur the precursor preparation process is simplified.But still need through in advance aqueous catalyst solution being scattered in the hydrocarbon ils-dehydration-sulfuration, and then join the process of advancing reactor reaction in the raw material.This invention claims that the catalyzer add-on is 50-300ppm, but add-on is 208ppm in the example.In all examples, all about 2.0w%, minimum is 1.8w% to its reaction process coking yield (Gu produce rate).This coking yield is obviously too high, is difficult in the actual production accept.
Existing patent and other technology of having reported all have higher green coke amount in the heavy-oil hydrogenation conversion process, the dehydration after catalyzer is dispersed in the heavy oil also has very big difficulty in actually operating.In addition, the frequent variation of oil product city field boundary also requires products scheme can change flexibly to adapt to city's field boundary.
The objective of the invention is to find a kind of method that aqueous solution catalyzer is directly used in hydrogenation of residual oil suspended bed, feasible weight, residual oil and catalyzer energy high dispersing, thereby can in the reactor that does not have the fixed beds layer, carry out hydrogenation and cracking reaction, make residual oil change into the lower boiling fraction in a large number, and the adding of catalyzer and the reaction process control requirement that can satisfy transformation efficiency both easy to operate can drop to the coking yield of reaction process below 1.0% again simultaneously.Another object of the present invention is to find a kind of working method that can adjust products scheme flexibly, thereby can distribute according to city's field boundary demand or according to the product of the flexible setting device of needs of upstream and downstream flow process.Further aim of the present invention is to find a kind of suitable method, and aqueous catalyst solution can economy be joined in the resid feed easily, carries out hydrogenation and cracking reaction in hydrogenator.
The present invention includes the following aspects: prepare the water-soluble catalyst that can be directly used in hydrogenation of residual oil suspended bed, but this catalyzer catalytic hydrogenation reaction not only, and can significantly suppress green coke.Contain elements such as Mo, Ni, P in the aqueous catalyst solution of preparing, Mo content is 2～15w%, better is 5～10w%, and Ni is 0.1～1w%, better is 0.2～1w%, and P is that 0.2～2w% better is 0.2～1w%.Aqueous catalyst solution is joined in the resid feed, and total metal add-on is 150～1500ppm, better is 200-1000ppm.Be separated into milk sap with ordinary method, enter reactor then.Fig. 1 is seen in the flow process signal.Process explanation is as follows:
Residual oil raw material and aqueous catalyst solution enter mixing tank 3 from pipeline 1 and 2 respectively.Mixing tank 3 can be a stirred pot, also can be a colloidal mill or static mixer or other conventional mixing equipment, and residual oil and aqueous catalyst solution are mixed.If material viscosity is big especially, be difficult to use the ordinary method mixing below 100 ℃, also can earlier aqueous catalyst solution be mixed with a small amount of long residuum, and then mix with full-bodied charging.Charging after mixing enters well heater 8 through pipeline 4 and pump 5, pipeline 7, and hydrogen enters system via pipeline 6.Charging is heated to 360-390 ℃ in process furnace 8, enter reactor 10 through pipeline 9 then.Reactor operating condition is hydrogen pressure 10～18MPa, feed liquid air speed 0.5～2h-1,390～460 ℃ of temperature of reaction, hydrogen-oil ratio 500～1500 (volume ratio).Reaction product enters high-pressure separator 12 via pipeline 11, tells gas and degass through pipeline 17 that body reclaims and separation system 18, and hydrogen can loop back reactor by pipeline 19 behind washing, purifying, and light oil goes out device through pipeline 20.The liquid material that high-pressure separator 12 is told enters a solid separating device 14 through pipeline 13, and solids constituent also can be used separating centrifuge from adopting filter method, and the liquid product of removing behind catalyst fines and the coke goes out system via pipeline 16.The solid materials that leaches can loop back reactor, also can go to the metal recovery system.
When feeding temperature higher (for example residual oil raw material is directly from upstream device), when being unsuitable for before charging, be mixed with very big difficulty with aqueous catalyst solution before entering system with aqueous solution.The present invention adopts the directly method of the injecting catalyst aqueous solution in feeding line, and Fig. 2 is seen in the flow process signal.From the warm sludge oil of pipeline 4 introducings from upstream device.Aqueous catalyst solution is squeezed into by pump 3, through a sparger 5 aqueous solution is spurted in the residual oil, and residual oil is in flow process catalyst neutralisation aqueous solution.High pressure hydrogen mixes the back by pipeline 6 introducings and sends into well heater 8 by pipeline 7 with residual oil, the charging that is heated to temperature of reaction is introduced reactors 10 by pipeline 9, at 8～17MPa, carries out hydrogenation reaction under 380～460 ℃ of conditions.Reaction product enters high-pressure separator 12 by pipeline 11, tells gas and degass through pipeline 17 that body reclaims and separation system 18, and hydrogen loops back reactor by pipeline 19 behind washing, purifying, and light oil goes out device through pipeline 20.The liquid material that high-pressure separator 12 is told enters a solid separating device 14 through pipeline 13, and solids constituent be from adopting filter method, also can be with a separating centrifuge, and the liquid product that leaches behind little amount of catalyst powder and the coke goes out system via pipeline 16.The solid materials that leaches can loop back reactor by pipeline 15, also can go to the metal recovery system.
When sulphur content in the residual oil raw material when not being low especially (for example content is less than 2.0w%), all can save and add vulcanizing agent prevulcanized step, and the residual oil sulphur content that generally needs hydrotreatment is mostly more than 2.0w%.
Advantage compared with prior art of the present invention is: 1. introduce the Ni element in P, Mo water-soluble catalytic agent prescription, suppressed green coke effectively.2. Mo/Ni atomic ratio and concentration can be adjusted the product distribution in the adjustment aqueous catalyst solution, thereby make production change products scheme flexibly according to city's field boundary demand and upstream and downstream requirements of process.3. total metal concentration can in catalyst metal add-on one regularly, reduce the moisture content of bringing in the charging up to 16w% in the aqueous solution, thereby can save the bigger step of this operation easier of dehydration, and the green coke amount still can be controlled in below the 1.0w%.4. can save the prevulcanized step that adds vulcanizing agent.
For further specifying all main points of the present invention, enumerate following examples.
The main influence of investigating the adding of nickel to the residual hydrogenation process of this test.Load weighted industrial molybdenum oxide (or phospho-molybdic acid), phosphoric acid, basic nickel carbonate are put into container, add water and be modulated into the aqueous catalyst solution that contains Mo, Ni, P. Wherein embodiment 2,5,7 uses phospho-molybdic acid.
Take by weighing isolated island vacuum residuum 250g and put into the autoclave that a 750mL band stirs, the aqueous catalyst solution that adds specified amount makes the total metal add-on of catalyzer account for the 200PPm of resid feed.Closed reactor, room temperature is filled hydrogen pressure to 7MPa behind the logical hydrogen exchange, begins then to stir to heat up, and reacts 1h down at 440 ℃.Reaction product surveys coking yield respectively, less than 350 ℃ of fractions (AGO) and 350-500 ℃ of fraction (VGO) yield, test-results sees Table 1.
The aqueous catalyst solution of table 1 different Mo, Ni, P proportioning is used for the residual hydrogenation test-results
| Embodiment | ????1 | ????2 | ????3 | ????4 | ????5 | ????6 | ????7 | ????8 |
| ????Mo | ????5.6 | ????5.6 | ????5.6 | ????10 | ????10 | ????10 | ????10 | ????10 |
| ????Ni | ????0 | ????0.2 | ????0.4 | ????0 | ????0.6 | ????0.8 | ????0.9 | ????1.0 |
| ????P/Mo | ????0.15 | ????0.15 | ????0.15 | ????0.087 | ????0.087 | ????0.10 | ????0.087 | ????0.087 |
| Green coke amount % | ????1∶69 | ????0.67 | ????0.10 | ????8.27 | ????4.65 | ????3.11 | ????1.18 | ????0.50 |
| ????AGO％ | ????32.69 | ????32.60 | ????32.54 | ????45.54 | ????42.29 | ????41.21 | ????40.16 | ????40.13 |
| ????VGO％ | ????31.34 | ????31.95 | ????32.34 | ????25.66 | ????29.33 | ????30.55 | ????31.22 | ????31.78 |
Even P, Mo atomic ratio have only 0.087 (P of industrial phospho-molybdic acid, Mo atomic ratio are 0.087-0.10) in the test-results explanation aqueous solution, molybdenum content also can make reaction process green coke amount be controlled at below the 1w% up to 10w% if suitably adjust nickel content.
Process of the test is with example 1.The catalyzer composition is suitably adjusted in this test explanation and reaction conditions can in very large range change the product distribution, makes production process have very big handiness.Reaction result sees Table 2 under different catalysts aqueous solution composition and the different tests condition.
Table 2
| Embodiment | ????9 | ????10 | ????11 | ????12 | ????13 | ????14 | ??????15 | ????16 |
| The aqueous solution is formed | ||||||||
| ??Mo??w％ | ????5.6 | ????4.0 | ????4.9 | ??4.9 | ????3.5 | ????2.0 | ????8.0 | ????6.4 |
| ??Ni??w％ | ????0.7 | ????0.3 | ????0.4 | ????1 | ????1 | ????0.1 | ????0.8 | ????1.0 |
| ??P/Mo | ????0.087 | ????0.087 | ????0.087 | ??0.087 | ????0.087 | ??0.087 | ????0.087 | ????0.087 |
| Reaction conditions | ||||||||
| Temperature of reaction ℃ | ????430 | ????440 | ????450 | ??390 | ????430 | ??440 | ????430 | ????430 |
| Reaction times, h | ????1 | ????1 | ????1 | ????2 | ????2 | ????3 | ????1 | ????2 |
| Catalyzer, ppm | ????160 | ????1450 | ????250 | ??300 | ????250 | ??427 | ????250 | ????250 |
| Reaction result | ||||||||
| Green coke amount w% | ????0.02 | ????0.446 | ????0.94 | ??0.03 | ????0.27 | ??0.98 | ????0.1 | ????0.67 |
| AG0 yield w% | ????33.0 | ????30.1 | ????47.3 | ??16.1 | ????36.8 | ??40.8 | ????35.5 | ????37.6 |
| VGO yield w% | ????31.2 | ????36.3 | ????28.0 | ??18.0 | ????43.9 | ??45.1 | ????29.9 | ????39.6 |
The hydrogenation of residual oil suspended bed reaction that the explanation of this example is carried out on continuous experimental apparatus.
Fig. 1 is seen in the signal of hydrogenation of residual oil suspended bed continuous apparatus.Residual oil raw material and aqueous catalyst solution mix in mixing tank 3.Charging after mixing enters well heater 8 through pipeline 4 and pump 5, pipeline 7, and hydrogen enters system via pipeline 6.Charging is heated to 360-390 ℃ in process furnace, enter reactor 10 through pipeline 9 then.Reaction product enters high-pressure separator 12 via pipeline 11, tells gas and degass through pipeline 17 that body reclaims and separation system 18, and hydrogen loops back reactor by pipeline 19 behind washing, purifying, and light oil goes out device through pipeline 20.The liquid material that high-pressure separator is told enters a solid separating device 14 through pipeline 13, and the liquid product that leaches behind little amount of catalyst powder and the coke goes out system via pipeline 16.The solid materials that leaches can loop back reactor, also can go to the metal recovery system.Operational condition and reaction result see Table 3.
Table 3
| Embodiment | ??17 | ????18 | ????19 | ????20 | ????21 | ????22 |
| Catalyzer is formed | ||||||
| ??Mo.??w％ | ??5.2 | ????5.2 | ????10.0 | ????14.0 | ????5.28 | ????5.28 |
| ??Ni，w％ | ??0 | ????0 | ????0.8 | ????1.0 | ????0.4 | ????0.4 |
| ????P/Mo | ??0.087 | ????0.087 | ????0.087 | ????0.087 | ????0.087 | ????0.087 |
| Reaction conditions | ||||||
| Reaction pressure MPa | ??14 | ????14 | ????14 | ????14 | ????14 | ????14 |
| Air speed, h -1 | ??1 | ????1 | ????1 | ????1 | ????1 | ????1 |
| Temperature, ℃ | ??430 | ????440 | ????395 | ????455 | ????440 | ????420 |
| Metal add-on PPm | ??450 | ????450 | ????400 | ????400 | ????450 | ????400 |
| Coking yield, % | ??1.5 | ????2.2 | ????0.25 | ????1.0 | ????0.72 | ????0.21 |
| ??AGO，％ | ??31.5 | ????34.1 | ????20.1 | ????37.1 | ????36.0 | ????33.2 |
| ??VGO，％ | ??29.5 | ????30.2 | ????22.5 | ????33.2 | ????32.8 | ????28.3 |
Example 23～26
This example explanation is when feeding temperature is higher feeding in raw material and reaction process when being unsuitable for before charging with aqueous solution.When feeding temperature higher (for example residual oil raw material is directly from upstream device), be mixed with very big difficulty with aqueous catalyst solution before entering system.The present invention adopts the directly method of the injecting catalyst aqueous solution in feeding line, and Fig. 2 is seen in the flow process signal.
From the warm sludge oil of pipeline 4 introducings from upstream device.Aqueous catalyst solution is squeezed into by pump 3, through a sparger aqueous solution is spurted in the residual oil, and residual oil is in flow process catalyst neutralisation aqueous solution.High pressure hydrogen is introduced by pipeline 6 and well heater 8 is sent into by pipeline 7 in residual oil mixing back.The charging that is heated to temperature of reaction is introduced reactor 10 by pipeline 9, at 8～17MPa, carries out hydrogenation reaction under 380～460 ℃ of conditions.Reaction product enters high-pressure separator 12 by pipeline 11, and subsequent process is with example 17～22.Test-results sees Table 4.
Table 4
| Embodiment | ????23 | ????24 | ????25 | ????26 |
| Mo.??w％ | ????5.2 | ????5.28 | ????10.0 | ????10.0 |
| Ni，??w％ | ????0 | ????0.4 | ????0.8 | ????0.8 |
| ????P/Mo | ????0.087 | ????0.087 | ????0.087 | ????0.087 |
| Reaction conditions | ||||
| Reaction pressure MPa | ????14 | ????14 | ????14 | ????14 |
| Air speed, h -1 | ????1 | ????1 | ????1 | ????1 |
| Temperature, ℃ | ????430 | ????440 | ????410 | ????440 |
| Metal add-on PPm | ????450 | ????350 | ????250 | ????300 |
| Coking yield, % | ????1.6 | ????0.57 | ????0.30 | ????0.49 |
| AGO，％ | ????32.6 | ????36.5 | ????31.8 | ????40.8 |
| VGO，??％ | ????31.7 | ????33.2 | ????34.6 | ????31.9 |
Claims (8)
1. suspension bed residual oil hydrogenation cracked method, it is characterized in that directly adopting the aqueous solution of Mo, Ni isoreactivity metal as catalyzer, this aqueous solution directly and after the residual oil raw material Hybrid Heating enters suspended-bed reactor, the aqueous catalyst solution add-on, count 150-1500ppm with reactive metal, at 380～460 ℃, carry out hydrocracking reaction under 10～15MPa hydrogen pressure.
2. according to the residual oil hydrocracking process of claim 1, it is characterized in that containing Mo2～15W% in the described aqueous catalyst solution Ni0.1～2W%, P0.1～3w%.
3. according to the residual oil hydrocracking process of claim 1, it is characterized in that resid feed directly with the aqueous catalyst solution mixing, mixed resid feed enters conversion zone and carries out hydrocracking and need not make catalyst precursor earlier.
4. according to the residual oil hydrocracking process of claim 1, it is characterized in that when raw material is cold feed, directly mix, mix hydrogen then, enter reactor after advancing the process furnace heating with aqueous catalyst solution.
5. according to the residual oil hydrocracking process of claim 1, it is characterized in that working as raw material directly from upstream device, when temperature was higher, aqueous catalyst solution was squeezed into hot oil line by a sparger by pump, advances reaction system again.
6. according to the residual oil hydrocracking process of claim 1, it is too high 100 ℃ of left and right sides viscosity to it is characterized in that working as raw material, when being unsuitable for directly mixing with aqueous catalyst solution, earlier with aqueous catalyst solution with a small amount of low viscous residual oil pre-mixing, and then mix with full-bodied reaction raw materials or join in the full-bodied resid feed by sparger.
7. according to the residual oil hydrocracking process of claim 1, the content that it is characterized in that metal M o, Ni and element P in the aqueous catalyst solution distributes according to technology and product and requires to adjust, and Mo content is 5～10w% in the aqueous catalyst solution; Ni content is 0.2～1w%; P content is 0.2～1w%.
8. according to the residual oil hydrocracking process of claim 1, it is characterized in that the add-on of aqueous catalyst solution, count 200-1000ppm with reactive metal.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95118354A CN1045307C (en) | 1995-11-22 | 1995-11-22 | Hydrocracking process of heavy oil and residual oil in suspension bed |
| CA002190404A CA2190404C (en) | 1995-11-22 | 1996-11-15 | A dispersing-type catalyst for hydrocracking of heavy oil and residuum, the preparation and the use thereof |
| US08/754,877 US5948721A (en) | 1995-11-22 | 1996-11-22 | Dispersing-type catalyst for hydrocracking of heavy oil and residuum, and a method for the preparation thereof |
| US09/204,050 US6004454A (en) | 1995-11-22 | 1998-12-02 | Hydrocracking of heavy oil and residuum with a dispersing-type catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95118354A CN1045307C (en) | 1995-11-22 | 1995-11-22 | Hydrocracking process of heavy oil and residual oil in suspension bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1158883A true CN1158883A (en) | 1997-09-10 |
| CN1045307C CN1045307C (en) | 1999-09-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95118354A Expired - Lifetime CN1045307C (en) | 1995-11-22 | 1995-11-22 | Hydrocracking process of heavy oil and residual oil in suspension bed |
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| Country | Link |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098337C (en) * | 2000-11-02 | 2003-01-08 | 中国石油天然气股份有限公司 | Normal pressure suspension bed hydrogenation process adopting liquid multiple-metal catalyst |
| CN1101457C (en) * | 1997-12-08 | 2003-02-12 | 中国石油化工集团总公司抚顺石油化工研究院 | Treatment method for inferior heavy and residual oil |
| CN101962571A (en) * | 2010-10-29 | 2011-02-02 | 大连理工大学 | Coal tar heavy fraction suspension-bed hydrocracking method and system thereof |
| CN101890380B (en) * | 2009-05-19 | 2011-12-21 | 中国石油化工股份有限公司 | Hydrodesulfurization catalyst and application thereof |
| CN106513049A (en) * | 2016-11-25 | 2017-03-22 | 青岛大学 | Heavy oil hydrofining nano-catalyst with ultrahigh coke inhibiting performance and preparation method and application of heavy oil hydrofining nano-catalyst |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1754770B1 (en) * | 2005-08-16 | 2017-01-18 | Research Institute of Petroleum | Process for hydroconverting of a heavy hydrocarbonaceous feedstock |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4913799A (en) * | 1984-12-18 | 1990-04-03 | Uop | Hydrocracking catalysts and processes employing non-zeolitic molecular sieves |
| CA1317585C (en) * | 1988-02-02 | 1993-05-11 | Chandra Prakash Khulbe | Hydrocracking of heavy oils in presence of iron-coal slurry |
| US5039392A (en) * | 1990-06-04 | 1991-08-13 | Exxon Research And Engineering Company | Hydroconversion process using a sulfided molybdenum catalyst concentrate |
-
1995
- 1995-11-22 CN CN95118354A patent/CN1045307C/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1101457C (en) * | 1997-12-08 | 2003-02-12 | 中国石油化工集团总公司抚顺石油化工研究院 | Treatment method for inferior heavy and residual oil |
| CN1098337C (en) * | 2000-11-02 | 2003-01-08 | 中国石油天然气股份有限公司 | Normal pressure suspension bed hydrogenation process adopting liquid multiple-metal catalyst |
| CN101890380B (en) * | 2009-05-19 | 2011-12-21 | 中国石油化工股份有限公司 | Hydrodesulfurization catalyst and application thereof |
| CN101962571A (en) * | 2010-10-29 | 2011-02-02 | 大连理工大学 | Coal tar heavy fraction suspension-bed hydrocracking method and system thereof |
| CN106513049A (en) * | 2016-11-25 | 2017-03-22 | 青岛大学 | Heavy oil hydrofining nano-catalyst with ultrahigh coke inhibiting performance and preparation method and application of heavy oil hydrofining nano-catalyst |
| CN106513049B (en) * | 2016-11-25 | 2018-12-28 | 青岛大学 | A kind of heavy-oil hydrogenation nanocatalyst and its preparation method and application pressing down burnt performance with superelevation |
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| CN1045307C (en) | 1999-09-29 |
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Owner name: CHINA PETROCHEMICAL CORPORATION; CHINA PETROLEUM & Free format text: FORMER NAME OR ADDRESS: CHINA PETRO-CHEMICAL CORP.; FUSHUN PETROCHEMICAL INSTITUTE., CHINA PETROCHEMICAL CORP. |
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Patentee after: China Petrochemical Group Corp. Patentee after: Sinopec Group Fushun Research Institute of Petroleum and Petrochemicals Patentee before: China Petrochemical Corporation Patentee before: Fushun Research Inst. of Petroleum Processing, China Petro-chem. Corp. |
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