CN1025216C - Process for conversion of hydrocarbonaceous feedstock - Google Patents
Process for conversion of hydrocarbonaceous feedstock Download PDFInfo
- Publication number
- CN1025216C CN1025216C CN 89109758 CN89109758A CN1025216C CN 1025216 C CN1025216 C CN 1025216C CN 89109758 CN89109758 CN 89109758 CN 89109758 A CN89109758 A CN 89109758A CN 1025216 C CN1025216 C CN 1025216C
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- Prior art keywords
- charging
- zeolite
- hydrocracking
- hydrotreatment
- catalyst
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Classifications
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
A process for the conversion of a hydrotreated and/or hydrocracked hydrocarbonaceous feedstock, such as a heavy flashed distillate or deasphalted oil, comprises contacting the feedstock with a zeolitic catalyst which comprises a zeolite with a pore diameter of 0.4 to 0.7 nm at a temperature above 480 .degree.C and a pressure of up to 10 bar for less than 10 seconds.
Description
The invention relates to a kind of method for transformation of hydrocarbon feed, particularly about the improvement of some hydrocarbon feed.
U.S. Pat 4171257 has been narrated a kind of method, and this method is by being lower than 14 crust at pressure, and it is under the condition of 0.1-15 liter/liters per hour charging to be contacted to improve hydrocarbon feed with ZSM-5 crystal aluminosilicate catalyzer with air speed that temperature is 260-427 ℃.Charging is 230-437 ℃ a gas oil as boiling range, must contain the nitrogenous compound (in nitrogen) that is less than 5ppmw.The product of improvement comprises alkene, as propylene and butylene.
Compare with the lower paraffin hydrocarbons of low value, the production of alkene is needed, because the reactivity of alkene makes it be suitable for changing into other product., this process has shortcoming, and promptly in order to avoid rapid catalyst deactivation, initial charge must be through strict denitrogenation.
Our surprised discovery uses some zeolite catalyst can obtain higher olefins yield under high temperature and short charging residence time under the not too strict condition of nitrogen content.And we are suitable for the heavy hydrocarbon charging at this conversion of also surprised discovery, and can obtain the improvement product of rich light alkene thus.
Therefore, the invention provides the method for transformation of the heavy hydrocarbon charging of a kind of hydrotreatment and/or hydrocracking.This method is included in temperature and is higher than under 480 ℃ and the pressure conditions up to 10 crust, and charging is that the zeolite catalyst of the zeolite of 0.4-0.7nm contacted in the time that was less than for 10 seconds with containing the aperture.
Charging contacts with zeolite catalyst and was less than for 10 seconds, and be 0.1 second duration of contact the shortest.Charging contacts the result that time of 1 to 6 second obtains with zeolite catalyst best.
Temperature is quite high in reaction process, yet the high temperature and the short residence time combine and obtained higher olefin conversion.Preferred temperature range is 480-900 ℃, preferably 500-750 ℃.
Zeolite catalyst contains the zeolite that a kind of aperture is 0.4-0.7nm.This catalyzer also should contain a kind of refractory oxides as tackiness agent.The refractory oxides that is fit to comprises: aluminum oxide, silicon-dioxide, silica-alumina, magnesium oxide, titanium oxide, zirconium white and their mixture.What preferentially select for use is aluminum oxide.The suitable weight ratio scope of refractory oxides and zeolite is 10: 90 to 90: 10, is preferably 50: 50-85: 15 these catalyzer can contain the zeolite of other aperture greater than 0.7nm.The example that this zeolite is fit to comprises: faujasite zeolitic, β zeolite, omega zeolite be X zeolite and Y zeolite particularly.Zeolite catalyst preferably contains the aperture and only is the zeolite of 0.4-0.7nm basically.
Term in this specification sheets " zeolite " is not considered to only comprise crystalline aluminosilicate, this term also comprises: crystalline silica (silicate (Silicalite)), aluminosilicophosphate (SAPO), the silicochromium hydrochlorate, silicic acid gallium, ferric metasilicate, aluminum phosphate (ALPO), silicoaluminate titanium (TASO), borosilicate, phosphorus titanium aluminate (TAPO) and silicoaluminate iron.
Can be used for method of the present invention, and have the example of the zeolite in 0.4-0.7nm aperture to comprise: SAPO-4 described in the US4440871 and SAPO-11; ALPO-11 described in the US4310440; TAPO-11 described in the US4500651; TASO-45 described in the EP-A-229295; Borosilicate described in the US-A-4254297; Resemble erionite, ferrierite, the pure aluminium silicate that Q type zeolite (thetd) is such and, ZSM-11, ZSM-12, ZSM-35, the ZSM-type zeolite that ZSM-23 and ZSM-38 are such as ZSM-5.Preferred zeolite is selected from the crystal metal silicate with ZSM-5 structure, ferrierite, erionite and their mixture.Suitable example with crystal metal silicate of ZSM-5 structure is at the pure aluminium silicate described in the GB-B-2110559, silicic acid gallium, ferric metasilicate, silicic acid
, silicic acid rhodium and/or scandium.
In the process of preparation zeolite, there is a large amount of alkalimetal oxides to be present in the zeolite that makes usually.The most handy known method of specialty of these basic metal removed, and for example uses ion exchange method, and roasting at random then obtains the zeolite of its hydrogen form.The used zeolite of present method preferably exists with its hydrogen form basically.
In the presence of no hydrogen or hydrogen donor, be easy to generate alkene.Therefore, present method is favourable under the adding that does not have hydrogen and/or steam.Certainly, in reaction process, might form some small molecules, as hydrogen molecule., these micromolecular amounts are normally ignored, and the 0.5%(that is generally less than product is heavy).
The pressure of this process can change in big scope.But this pressure is preferably in charging is existed with its gas phase form substantially.So just be easier to reach the short contacting time of expectation.Therefore, pressure is preferably lower.Owing to do not need expensive compressor and high pressure vessel and other necessary equipment, so present method more has superiority.Used pressure can be up to 10 crust.But pressure is pressure below atmospheric pressure also, but this is not preferred.Minimum pressure can be 1 crust.Under barometric point, operate not only economy but also favourable.
The weight ratio of catalyzer/charging can change bigger, and for example every kg feed can have and is higher than 200 kilograms catalyzer.The weight ratio of catalyzer/charging is preferably 2-200.
Process of the present invention can be carried out in fixed bed, but this means the short contacting time that needs high air speed to reach expectation.Therefore, this process is preferably in the moving-bed and carries out.Catalyst bed can move up or down.When bed moved up, the process that obtains was similar to fluid catalytic cracking process.This process is preferably in to move down in the bed carries out.
Some coke in this process, on catalyzer, have been generated.Therefore, be necessary regenerated catalyst.Catalyzer is with after charging contacts, and the available oxygen oxidizing gases makes its regeneration as the air handling catalyzer.Preferably use cyclic regeneration, the regeneration that promptly is similar in fluid catalytic cracking process to be carried out.
Owing under very high flow velocity, can not form coke, therefore, can use a kind of like this process, the residence time of granules of catalyst in reaction zone (as moving-bed) is longer than the residence time of charging in reaction zone in this process.Certainly, should be less than for 10 seconds the duration of contact of charging and catalyzer.The residence time common and charging duration of contact adapts.The catalyzer residence time that is fit to is 1-20 a times of the charging residence time.
The charging that will be transformed comprises the hydro carbons of hydrotreatment and/or hydrocracking in the method, preferably heavy feedstocks (though this is unnecessary).The charging that is fit to is to obtain by hydrotreatment and/or the following oil of hydrocracking, i.e. heavy flash distillation oil separation that is obtained by long residuum or the deasphalted oil that is obtained by vacuum residuum.The method according to this invention, charging after hydrotreatment and/or hydrocracking with carry out suitable fractionation before zeolite catalyst contacts to remove low boiling range cut.
The product that method of the present invention obtains selectively carries out fractionation, to obtain rich olefins gas fraction, gasoline fraction and tower bottom distillate.The all or part of charging upstream section that selectively is recycled to hydrotreatment and/or hydroeracking unit of these cuts.Like this, heavy deasphalted oil or heavy flash distillation oil separation have changed into more valuable rich olefins gas than the highland.
Therefore, another aspect of the present invention has provided a kind of method that transforms hydrocarbon feed, this method comprises: hydrotreatment and/or the above-mentioned charging of hydrocracking in the presence of the catalyzer that is fit to, temperature be higher than 480 ℃ with pressure up to 10 crust under the product of near small part hydrotreatment and/or hydrocracking contact with zeolite catalyst (containing the zeolite that the aperture is 0.4-0.7nm) and be less than for 10 seconds, the transformation substance that fractionation obtains, and heavy ends is recycled to above-mentioned hydrotreatment and/or hydrocracking step.
Above-mentioned hydrotreating step is known in the prior art, and can carry out under known condition.The condition that is fit to comprises that temperature is 150-400 ℃, and hydrogen (branch) is pressed the crust for 30-150, and air speed is the 0.5-4.0 kg/liter, hour, hydrogen/charging is 100-2000Nl/Kg.The hydrotreating catalyst that is fit to comprises nickel, cobalt, tungsten, molybdenum, platinum, palladium or their mixture that is loaded on the carrier, and carrier comprises as aluminum oxide, silica-alumina, silicon-dioxide, zirconium white, zeolite etc.This catalyzer also can contain fluorine, phosphorus and/or boron.These professional those skilled in the art can select temperature, gas velocity and air speed from the above-mentioned suitable scope that provides.
Hydrocracking also is known in the prior art, and can to carry out under known condition be 300-450 ℃ in temperature for example, and hydrogen (branch) is pressed to 50-200 clings to, and air speed is 0.5-2.0kg/l, catalyzer, hour.H
2/ mineral oil fractions is to carry out on hydrocracking catalyst under the 500-2000Nl/kg condition.Hydrocracking catalyst can be selected from any hydrocracking catalyst well known in the prior art.The hydrocracking catalyst that is fit to contains a kind of carrier and at least a hydrogenation metal or its compound, and this carrier is to be selected from silicon-dioxide, aluminum oxide, silica-alumina and faujasite zeolitic, and faujasite zeolitic is Y zeolite preferably.Best hydrogenation metal is nickel, cobalt, tungsten and molybdenum and composition thereof, and platinum and palladium also can use.This catalyzer also contains fluorine and/or phosphorus and/or boron.When using nickel, cobalt, molybdenum and/or tungsten as hydrogenation metal, they preferably exist with the form of its sulfide.
Compare with the method for U.S. Pat 4171257, one of advantage of the present invention is to use nitrogen content to be higher than the charging of 5ppmw, and activity of such catalysts is not had influence substantially.The charging that is fit to can have more than 10ppmw(in nitrogen) nitrogen content, this charging even can contain 1000ppmw or higher nitrogen content (in nitrogen).
Further narrate the present invention by reference the following example and accompanying drawing now.
Embodiment 1
Charging in the present embodiment is the Arabic lightweight deasphalted oil with hydrotreatment of following character:
IBP，℃ 453
50%(weight) 591
67%(weight) 620
Proportion 70/4 0.8532kg/l
Sulphur 232ppmw
Nitrogen 12ppmw
By making diasphaltene charging and catalyst stream and flowing to down, make this charging in downflow reactor, obtain improvement.Catalyst system therefor is to contain ZSM-5(weight ratio ZSM-5 in alumina substrate: aluminum oxide is 1: 3).Experiment is to carry out under normal pressure.Other operational conditions and experimental result are listed in the table below in 1.
Table 1
Operational condition
Temperature of reactor, ℃ 531
Catalyst/oil gram/gram 4.3
Second 2.2 duration of contact
Product % weight (with feed charging meter)
C
11.0
C
21.2
C
- 24.9
C
32.0
C
- 317.9
C
42.1
C
- 416.4
C
5-221℃ 26.3
221-450℃ 18.2
450℃
+9.1
Coke 0.8
450 ℃
+The transformation efficiency 91 of charging
From The above results as can be seen, a large amount of gaseous product are that alkene is undersaturated, and product contains relatively large middle runnings.
Embodiment 2:
Charging in the present embodiment is the heavy flash distillation oil separation with hydrocracking of following character:
IBP，℃ 330
50%(weight) 432
FBP，℃ 620
Boiling point is lower than 370 ℃ cut %(weight) 7.7
Proportion 70/4 0.8157kg/l
Sulphur 20ppmw
Nitrogen 2ppmw
Present embodiment carries out under the condition described in the embodiment 1, but used operational condition lists in the following table 2, and what obtain the results are shown in the table 2.
Table 2
Operational condition:
Temperature of reactor ℃ 579
Catalyst/oil g/g 141
Second 1.7 duration of contact
Product %(is with feed charging meter)
C
11.6
C
21.0
C
- 214.7
C
33.9
C
3C
- 337.3
C
44.6
C
- 418.8
C
5-221℃ 8.6
221-370℃ 2.3
370℃
+0.4
Coke 6.3
370 ℃
+The transformation efficiency %(weight of charging) 99.6
Embodiment 3
Present embodiment uses Arabic heavy flash distillation oil separation as charging, and through after the initial hydrocracking, products therefrom generally has the 3 given character of tabulating down.
The flash distillation distillate is handled with following process shown in Figure 1.
Charging is introduced by pipeline 1, and with enter hydrotreatment/hydroeracking unit 3 after the hydrogen of pipeline 2 mixes, device 3 is to be 90 to cling in the hydrogen dividing potential drop, temperature is 400 ℃ and suitable Ni/M is housed.Operate under the condition of/aluminum oxide hydrotreating catalyst.
Hydrotreatment products is fractionated into gaseous fraction 5, gasoline fraction 6, kerosene(oil)fraction 7, gas oil fraction 8 and tower bottom distillate 9 in device 4.Under described condition, tower bottom distillate 9 is sent in the embodiment 1 described downflow reactor 10, and downflow reactor 10 contains embodiment 1 described catalyzer, and has suitable regenerating unit, if desired, coke can be removed from regenerating unit by pipeline 11.And gaseous state and liquid product are fractionated into gaseous product 13 in fractionation plant 12, and gasoline product 14 and tower base stream 15, this tower base stream 15 are recycled in the pipeline 1 to mix with charging and reprocess.
When fractionation in device 12, the tower bottom distillate 9 of improvement accounts for the 69%(weight of initial charge in the pipeline 1 in reactor 10).List in the following table 3 by device 12 fractions consistings that obtain.
Table 3
The hydrocracking charging
Specific refractory power, n
20 D1.4720
UV aromatic hydrocarbon, mmol/100g
Single 25
24
Many 3
Initial boiling point, ℃ 340
50%(weight) 420
Full boiling point 540
Product, %(weight) (with feed charging meter)
Gas (C
1-4) 31.5
H
20.1
C
10.7
C
20.8
C
- 23.4
C
31.4
C
- 312.3
C
41.5
C
411.3
Gasoline (C
5-221 ℃) 18.5
Coke 0.5
Reflux (221
+℃) 19
From The above results as can be seen, produced unsaturated gaseous state product of a large amount of alkene and gasoline from the separating of oil tower bottom distillate oil that goes out of initial flash distillation cut, and recycle unit can improve farthest, obtains many valuable products.
Claims (9)
1, the method for transformation of the hydrocarbon feed of a kind of hydrotreatment and/or hydrocracking, this method is included in temperature and is higher than 480 ℃, pressure makes down charging be less than for 10 seconds with containing zeolite that the aperture is 0.4-0.7nm and contact as the zeolite catalyst of the heat-resisting oxygenant of tackiness agent up to 10 crust, wherein the weight ratio of refractory oxides and zeolite is 10: 90 to 90: 10, the weight ratio of catalyzer and charging is 2-200, obtains the unsaturated gaseous state product of alkene at high proportion.
2, according to the process of claim 1 wherein that charging contacts 1-6 second with zeolite catalyst.
3, according to the method for claim 1 or 2, wherein temperature is 480-900 ℃.
4, according to the method for claim 1 or 2, its mesolite is selected from crystal metal silicate, ferrierite, erionite and their mixture with ZSM-5 structure.
5, according to the method for claim 1 or 2, wherein zeolite exists with its hydrogen form substantially.
6, according to the method for claim 1 or 2, this method is to carry out under the situation of not hydrogenation or steam.
7, according to the method for claim 1 or 2, this method is to carry out in the downflow system moving-bed.
8, according to the method for claim 1 or 2, wherein charging is deasphalted oil or the heavy flash distillation oil separation after hydrotreatment and/or the hydrocracking.
9, according to the method for claim 1, the transformation substance that fractionation obtains, and heavy ends is recycled in described hydrotreatment and/or the hydrocracking step.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL8828206 | 1988-12-02 | ||
| GB888828206A GB8828206D0 (en) | 1988-12-02 | 1988-12-02 | Process for conversion of hydrocarbonaceous feedstock |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1043156A CN1043156A (en) | 1990-06-20 |
| CN1025216C true CN1025216C (en) | 1994-06-29 |
Family
ID=10647877
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 89109758 Expired - Fee Related CN1025216C (en) | 1988-12-02 | 1989-12-01 | Process for conversion of hydrocarbonaceous feedstock |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP0372632B1 (en) |
| JP (1) | JPH02212594A (en) |
| CN (1) | CN1025216C (en) |
| AU (1) | AU621169B2 (en) |
| BR (1) | BR8906158A (en) |
| CA (1) | CA2004390A1 (en) |
| DE (1) | DE68925574T2 (en) |
| ES (1) | ES2082769T3 (en) |
| GB (1) | GB8828206D0 (en) |
| PH (1) | PH27238A (en) |
| RU (1) | RU2017790C1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8529753B2 (en) | 2006-12-27 | 2013-09-10 | Research Institute Of Petroleum Processing, Sinopec | Combined process for hydrotreating and catalytic cracking of residue |
| US9260667B2 (en) | 2007-12-20 | 2016-02-16 | China Petroleum & Chemical Corporation | Combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
Families Citing this family (29)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8904408D0 (en) * | 1989-02-27 | 1989-04-12 | Shell Int Research | Process for the conversion of a hydrocarbonaceous feedstock |
| CN1034223C (en) * | 1993-03-29 | 1997-03-12 | 中国石油化工总公司 | Cracking catalyst for processing low-carbon olefines |
| CN1034586C (en) * | 1993-11-05 | 1997-04-16 | 中国石油化工总公司 | Catalytic conversion method of low-carbon olefines high-output |
| FR2778345B1 (en) * | 1998-05-06 | 2000-11-24 | Inst Francais Du Petrole | ZEOLITH-BASED CATALYST CONTAINING BORON AND / OR SILICON FOR USE IN HYDROCRACKING |
| FR2778343B1 (en) | 1998-05-06 | 2000-06-16 | Inst Francais Du Petrole | CATALYST BASED ON ZEOLITH Y NOT GLOBALLY DESALUMINATED, BORON AND / OR SILICON AND HYDROCRACKING PROCESS |
| BR9901875A (en) * | 1998-05-13 | 2000-05-09 | Inst Francais Du Petrole | Process for improving the flow point and catalyst based on at least one zeolite mtt, ton, fer. |
| US6835863B2 (en) | 1999-07-12 | 2004-12-28 | Exxonmobil Oil Corporation | Catalytic production of light olefins from naphtha feed |
| US6222087B1 (en) | 1999-07-12 | 2001-04-24 | Mobil Oil Corporation | Catalytic production of light olefins rich in propylene |
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| KR20200105409A (en) | 2019-02-28 | 2020-09-07 | 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 | Novel tetraaryl borate compounds, catalysts composition containing the same, and methods for preparing ethylene homopolymers or copolymers of ethylene and α-olefins using the same |
| KR20240045992A (en) | 2022-09-30 | 2024-04-08 | 사빅 에스케이 넥슬렌 컴퍼니 피티이 엘티디 | Transition metal compound, catalyst composition comprising the same, and method for preparing olefin polymer using the same |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3420770A (en) * | 1966-09-28 | 1969-01-07 | Mobil Oil Corp | Catalytic cracking of hydrocarbons |
| US3856659A (en) * | 1972-12-19 | 1974-12-24 | Mobil Oil Corp | Multiple reactor fcc system relying upon a dual cracking catalyst composition |
| US4171257A (en) * | 1978-10-23 | 1979-10-16 | Chevron Research Company | Petroleum distillate upgrading process |
| US4502945A (en) * | 1982-06-09 | 1985-03-05 | Chevron Research Company | Process for preparing olefins at high pressure |
| NL8301352A (en) * | 1983-04-18 | 1984-11-16 | Shell Int Research | PROCESS FOR THE PREPARATION OF LOW-ASPHALTENE HYDROCARBON MIXTURES. |
| EP0125709B1 (en) * | 1983-04-18 | 1989-08-02 | Shell Internationale Researchmaatschappij B.V. | A process for the production of low-asphaltenes hydrocarbon mixtures |
| ES2087073T3 (en) * | 1988-06-16 | 1996-07-16 | Shell Int Research | PROCEDURE FOR THE CONVERSION OF A HYDROCARBON FEEDING MATERIAL. |
-
1988
- 1988-12-02 GB GB888828206A patent/GB8828206D0/en active Pending
-
1989
- 1989-11-29 EP EP19890203038 patent/EP0372632B1/en not_active Revoked
- 1989-11-29 DE DE1989625574 patent/DE68925574T2/en not_active Revoked
- 1989-11-29 ES ES89203038T patent/ES2082769T3/en not_active Expired - Lifetime
- 1989-12-01 JP JP31084489A patent/JPH02212594A/en active Pending
- 1989-12-01 CN CN 89109758 patent/CN1025216C/en not_active Expired - Fee Related
- 1989-12-01 CA CA 2004390 patent/CA2004390A1/en not_active Abandoned
- 1989-12-01 AU AU45799/89A patent/AU621169B2/en not_active Ceased
- 1989-12-01 RU SU4742676 patent/RU2017790C1/en active
- 1989-12-04 BR BR8906158A patent/BR8906158A/en not_active Application Discontinuation
- 1989-12-08 PH PH39654A patent/PH27238A/en unknown
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8529753B2 (en) | 2006-12-27 | 2013-09-10 | Research Institute Of Petroleum Processing, Sinopec | Combined process for hydrotreating and catalytic cracking of residue |
| US9260667B2 (en) | 2007-12-20 | 2016-02-16 | China Petroleum & Chemical Corporation | Combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0372632A1 (en) | 1990-06-13 |
| AU4579989A (en) | 1990-06-07 |
| AU621169B2 (en) | 1992-03-05 |
| RU2017790C1 (en) | 1994-08-15 |
| BR8906158A (en) | 1990-07-31 |
| CN1043156A (en) | 1990-06-20 |
| CA2004390A1 (en) | 1990-06-02 |
| PH27238A (en) | 1993-05-04 |
| JPH02212594A (en) | 1990-08-23 |
| DE68925574T2 (en) | 1996-08-08 |
| EP0372632B1 (en) | 1996-01-31 |
| DE68925574D1 (en) | 1996-03-14 |
| ES2082769T3 (en) | 1996-04-01 |
| GB8828206D0 (en) | 1989-01-05 |
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