GB1560148A - Process for the conversion of hydrocarbons - Google Patents
Process for the conversion of hydrocarbons Download PDFInfo
- Publication number
- GB1560148A GB1560148A GB4836277A GB4836277A GB1560148A GB 1560148 A GB1560148 A GB 1560148A GB 4836277 A GB4836277 A GB 4836277A GB 4836277 A GB4836277 A GB 4836277A GB 1560148 A GB1560148 A GB 1560148A
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- Prior art keywords
- pbw
- residue
- stage
- carried out
- atmospheric
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/049—The hydrotreatment being a hydrocracking
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Description
(54) PROCESS FOR THE CONVERSION OF HYDROCARBONS
(71) We, SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V., a company organised under the laws of The Netherlands, of 30 Carel van Bylandtlaan, The
Hague, The Netherlands, do hereby declare the invention, for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement:
The invention relates to a process for the preparation of one or more atmospheric hydrocarbon oil distillates from an atmospheric hydrocarbon oil residue.
In the atmospheric distillation of crude mineral oil, as applied on a large scale in refineries for the preparation of atmospheric distillates, a residual oil is obtained as a by-product. In some cases this residual oil is suitable for use as the starting material in the preparation of lubricating oil, but generally the residual oil, which as a rule contains considerable quantities of sulphur, metals and asphaltenes, is only suitable for use as fuel oil.
In view of the increasing demand for atmospheric distillates, several processes were investigated in the past which were aimed at converting the residual oils into atmospheric distillates. Examples of such processes are catalytic cracking and hydrocracking. The use of the residual oils as such as the feed for these processes has considerable disadvantages which preclude their application on a commercial scale. Thus, a major drawback of catalytic cracking of the residual oils is that because of the very high coke and gas production only a low yield of the desired atmospheric distillates is obtained. Hydrocracking of the residual oils involves a very rapid catalyst deactivation and/or a very high gas production and/or a very high hydrogen consumption.
In view of the above and considering the fact that in the atmospheric distillation of crude mineral oil about half of the crude oil is left behind as distillation residue, it will be clear that there is an urgent need for a process which offers the possibility of converting atmospheric hydrocarbon oil residues in an economically justifiable way into atmospheric hydrocarbon oil distillates such as gasolines.
Since catalytic cracking and hydrocracking have proved in practice to be excellent processes for the conversion of heavy hydrocarbon oil distillates such as vacuum gas oils into light distillates such as gasolines, the Applicants have carried out an investigation to find out to what extent these processes can be employed in the conversion of the above-mentioned atmospheric residues. It has been found that by a proper combination of catalytic cracking and/or hydrocracking with a catalytic hydrotreatment and a deasphalting, a process can be realized that is highly suitable for this purpose. The present patent application relates to such a process.
In the process according to the invention an atmospheric hydrocarbon oil residue is subjected to a catalytic hydrotreatment and the hydrotreated product is separated by distillation into one or more atmospheric distillates, a vacuum distillate and a vacuum residue.
The vacuum residue is separated by deasphalting into a deasphalted oil and asphalt. The vacuum distillate and the deasphalted oil are converted by catalytic cracking and/or hydrocracking into one or more atmospheric distillates and at least 50 %w of the asphalt is again subjected to catalytic hydrotreatment. The catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt in a combined feed mixture should be carried out under such conditions that more than 50 %w of the asphalt present in the feed for the catalytic hydrotreatment is converted into material that does not precipitate in a deasphalting process carried out under the same conditions as the deasphalting of the vacuum residue.
The process according to the invention comprises catalytic cracking and/or hydrocracking of a vacuum distillate and a deasphalted oil as the main operation(s). In these operations a considerable proportion of the feed concerned is converted into the said atmospheric distillates. One or more atmospheric distillates are separated as end products from the cracked product by distillation. To increase the yield of atmospheric distillates it is preferred to recycle at least part of the atmospheric residue obtained in the distillation of the cracked product to the catalytic cracker or hydrocracker.If the process according to the invention comprises catalytic cracking and, in addition, at least part of the aforementioned atmospheric residue is recycled to the catalytic cracking unit and/or a deasphalted oil is used as the feed or as a feed component for the catalytic cracking unit, these liquids are preferably given a light catalytic hydrotreatment before they are subjected to catalytic cracking. In the catalytic cracking process, which is preferably carried out in the presence of a zeolitic catalyst, coke is deposited on the catalyst. This coke is removed from the catalyst by burning-off during a catalyst regeneration step that is combined with the catalytic cracking, whereby a waste gas is obtained which contains carbon monoxide and carbon dioxide.
Catalytic cracking is preferably carried out at an average temperature of from 400 to 5500C and in particular from 450 to 5250C, a pressure of from 1 to 10 bar and in particular from 1.5 to 7.5 bar, a space velocity of from 0.25 to 4 kg.kg-l.h-l and in particular from 0.5 to 2.5 kg.kg-'.h-l and a rate of catalyst replenishment of from 0.1 to 5 and in particular from 0.2 to 2 tonnes of catalyst per 1000 tonnes of feed.
The process according to the invention may comprise hydrocracking. Hydrocracking is effected by contacting the feed at elevated temperature and pressure and in the presence of hydrogen with a suitable hydrocracking catalyst. Hydrocracking is preferably carried out as a two-stage process, in which the hydrocracking proper, which is effected in the second stage, is preceded by a catalytic hydrotreatment which serves mainly to reduce the nitrogen and polyaromatics contents of the feed to be hydrocracked. Catalysts suitable for use in the single stage hydrocracking process as well as in the second stage of the two-stage hydrocracking process are moderately and strongly acidic catalysts comprising one or more metals having hydrogenation activity on a carrier.Catalysts suitable for use in the first stage of the two-stage hydrocracking process are weakly and moderately acidic catalysts comprising one or more metals having hydrogenation activity on a carrier. Hydrocracking is preferably carried out at an average temperature of from 250 to 450"C and in particular from 300 to 425"C, a hydrogen partial pressure of from 25 to 300 bar and in particular from 50 to 150 bar, a space velocity of from 0.1 to 10 kg.l-'.h-l and in particular from 0.25 to 2 kg.l-'.h-l and a hydrogen-to-feed ratio of from 200 to 3000 Nl.kg-' and in particular from 500 to 2000 Nl.kg'. If the hydrocracking is carried out according to the two-stage process it is preferred to use the whole reaction product from the first stage (without ammonia, hydrogen sulphide or other volatile components being separated from it) as the feed for the second stage.
The process according to the invention comprises an operation in which deasphalting is applied to the vacuum residue of the hydrotreated product. The deasphalting is preferably carried out at elevated temperature and pressure and in the presence of an excess of a lower hydrocarbon such as propane, butane or pentane.
The process according to the invention comprises a further operation in which a catalytic hydrotreatment is applied to a mixture of an atmospheric residue and asphalt. This catalytic hydrotreatment has to be carried out under such conditions that more than 50 %w of the asphalt present in the feed for the catalytic hydrotreatment is converted into material which does not precipitate in a deasphalting step effected under the same conditions as the deasphalting of the vacuum residue. This catalytic hydrotreatment is preferably carried out as a two-stage process, in which the conversion proper of asphalt, which conversion is effected in the second stage, is preceded by a catalytic hydrotreatment intended mainly to reduce the metal content of the feed to be converted.Catalysts suitable for use in the one-stage catalytic hydrotreatment as well as in the second stage of the two-stage catalytic hydrotreatment comprise one or more metals having hydrogenation activity on a carrier, which carrier consists of more than 40 %w alumina. Catalysts suitable for use in the first stage of the two-stage catalytic hydrotreatment consist of more than 80 %w silica. The catalytic hydrotreatment is preferably carried out at an average temperature of from 375 to 475"C and in particular from 390 to 450"C, a hydrogen partial pressure of from 25 to 300 bar and in particular from 50 to 200 bar, a space velocity of from 0.1 to 3.0 kg.l-|4.h-+ and in particular from 0.2 to 2.0 kg.l-'.h-' and a hydrogen-to-feed ratio of from 250 to 2500
Nl.kg-' and in particular from 500 to 2000 Nl.kg-'. If the catalytic hydrotreatment is carried out in two stages, the first stage is preferably effected in the presence of a quantity of
H2S corresponding to an H2S content of the gas at the reactor inlet of more than 10 %v and the second stage in the presence of a quantity of H2S corresponding to an H2S content of the gas at the reactor inlet of less than 5 Nov.
As stated hereinbefore, the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt in a combined feed mixture according to the invention has to be carried out under such conditions that more than 50 Wow of the asphalt present in the feed for the catalytic hydrotreatment is converted into products which do not precipitate in a deasphalting step effected under the same conditions as the deasphalting of the vacuum residue.
Among these products are atmospheric distillates which are suitable as end products.
In the process according to the invention two streams are obtained which have to be subjected to catalytic cracking or hydrocracking, viz. a deasphalted oil and a vacuum distillate. For the conversion of the two streams preference is given to the same treatment and to treatment in one unit.
The process according to the invention is suitable both for the preparation of exclusively one or more light distillates as the end products and for the preparation of one or more light distillates together with one or more middle distillates as the end products. If the aim is to prepare exclusively one or more light distillates as the end products, a middle distillate to be separated from the cracked product and having an initial boiling point above the final boiling point of the heaviest light distillate desired is also eligible for repeated cracking.In that case, besides the vacuum distillate of the hydrotreated product, a middle distillate to be separated from the hydrotreated product and having an initial boiling point above the final boiling point of the heaviest light distillate desired is also eligible for use as feed component for the catalytic cracking or hydrocracking to be carried out as the main operation.
A process scheme for the conversion of atmospheric hydrocarbon oil residues into light and medium hydrocarbon oil distillates will be described hereinafter in more detail by reference to the appended figure.
Process scheme (see figure)
The process is carried out in an apparatus comprising successively a catalytic hydrotreating section (1), the first atmospheric distillation section (2), a vacuum distillation section (3), a deasphalting section (4), a catalytic cracking section (5), and the second atmospheric distillation section (6). A hydrocarbon oil residue (7) obtained by atmospheric distillation is mixed with an asphalt (8) and the mixture, together with a hydrogen stream (9), is subjected to a catalytic hydrotreatment. After separation of a gas stream (10), substantially consisting of C4 hydrocarbons and H2S, from the hydrotreated product, the liquid reaction product (11) is separated by atmospheric distillation into a gasoline fraction (12), a middle distillate fraction (13) and a residue (14).The residue (14) is separated by vacuum distillation into a vacuum distillate (15) and a vacuum residue (16). The vacuum residue (16) is separated by deasphalting into a deasphalted oil (17) and an aslphalt (18). The asphalt (18) is separated into two portions (8) and (19) having the same composition. The vacuum distillate (15) is mixed with the deasphalted oil (17) and the mixture is catalytically cracked.
In the regeneration of the catalyst in the catalytic cracking unit a waste gas (20) is obtained which contains carbon monoxide and carbon dioxide. The catalytically cracked product
(21) is separated by atmospheric distillation into a C4 fraction (22), a gasoline fraction (23), a middle distillate fraction (24) and a residue (25) being a mixture of heavy cycle oil and slurry oil.
The present patent application also comprises an apparatus for carrying out the process according to the invention as schematically shown in the appended figure.
The process according to the invention was applied to an atmospheric distillation residue of a crude oil from the Middle East. The atmospheric distillation residue had an initial boiling point of 370"C. By vacuum distillation of 100 pbw of the atmospheric residue, 44 pbw of a 520 C+ vacuum residue could be separated from it; by deasphalting these 44 pbw vacuum residue at 145"C and 41 bar with butane as the solvent and a solvent-to-oil weight ratio of 4:1, 21 pbw of C4 asphalt could be obtained from it. The process was carried out according to the appended process scheme. The following conditions were used in the various sections.
The catalytic cracking was effected in the presence of a zeolitic catalyst at a temperature of 490"C, a pressure of 2.2 bar and a space velocity of 2 kg.kg- l.h- The catalytic hydrotreatment was effected in two stages in the presence of an Ni/V/SiO2 catalyst comprising 0.5 pbw nickel and 2 pbw vanadium per 100 pbw silica in the first stage, and an Ni/Mo/Al203 catalyst comprising 4 pbw nickel and 11 pbw molybdenum per 100 pbw alumina in the second stage.The first stage of the catalytic hydrotreatment was conducted at an average temperature of 420"C, a hydrogen partial pressure of 150 bar and a space velocity of 1.75 kg.1-l.h-l and a hydrogen-to-feed ratio of 1000 N1.kg-l. The second stage of the catalytic hydrotreatment was conducted at an average temperature of 425"C, a hydrogen partial pressure of 150 bar, a space velocity of 1.9 kg.1-l.h- and a hydrogen-tofeed ratio of 1500 Nl.kg-'.
The deasphalting was carried out at 1450C and 41 bar with butane as the solvent and at a solvent-to-oil weight ratio of 4:1.
EXAMPLE
With 100 pbw of the 3700C atmospheric distillation residue (7) as the starting material, the quantities of the various streams were as follows:
3.2 pbw hydrogen (9),
11.3 pbw C4 fraction + H2S (10), 102.6 pbw liquid product (11),
9.7 pbw Cs-2000C gasoline fraction (12),
18.2 pbw 200-370"C middle distillate fraction (13),
74.7 pbw 370 C+ residue (14),
39.4 pbw 370-520"C vacuum distillate (15),
35.3 pbw 520 C+ vacuum residue (16),
23.8 pbw deasphalted oil (17),
11.5 pbw asphalt (18),
10.7 pbw portion (8 0.8 pbw portion (19 9.7 pbw C4 fraction (22),
30.2 pbw C5-200 C gasoline fraction (23),
10.1 pbw 200-370"C middle distillate fraction (24), and
9.4 pbw 370 C+ residue (25).
WHAT WE CLAIM IS:
1. A process for the preparation of one or more atmospheric hydrocarbon oil distillates, characterized in that the preparation is effected, starting from a hydrocarbon oil residue obtained by atmospheric distillation, by catalytic cracking and/or hydrocracking in combination with a catalytic hydrotreatment and deasphalting that the atmospheric residue is subjected to the catalytic hydrotreatment, that the hydrotreated product is separated by distillation into one or more atmospheric distillates, a vacuum distillate and a vacuum residue, that the vacuum residue is separated by deasphalting into a deasphalted oil and asphalt, that the vacuum distillate and the deasphalted oil are converted by catalytic cracking and/or hydrocracking into one or more atmospheric distillates, that at least 50 %w of the asphalt with the hydrocarbon oil residue in a combined feed mixture is again subjected to catalytic hydrotreatment and that the catalytic hydrotreatment is carried out under such conditions that more than 50 Sow of the asphalt present in the feed for the catalytic hydrotreatment is converted into material that does not precipitate in a deasphalting step carried out under the same conditions as the deasphalting of the vacuum residue.
2. A process according to claim 1, characterized in that at least part of the residue obtained in the atmospheric distillation of the catalytically cracked or hydrocracked product is recycled to the cracking unit concerned.
3. A process according to claim 1 or 2, characterized in that catalytic cracking is applied, that part of the residue of the cracked product is recycled to the catalytic cracking unit and/or that a deasphalted oil is used as the feed for the catalytic cracking unit and that these liquids are given a light catalytic hydrotreatment before they are subjected to catalytic cracking.
4. A process according to any one of claims 1-3, characterized in that catalytic cracking is carried out at an average temperature of from 400 to 550"C, a pressure of from 1 to 10 bar, a space velocity of from 0.25 to 4 kg.kg-3.h-3 and a rate of catalyst replenishment of from 0.1 to 5 tonnes of catalyst per 1000 tonnes of feed.
5. A process according to any one of claims 1-4, characterized in that hydrocracking is carried out as a two-stage process in the presence of a weakly or moderately acidic catalyst comprising one or more metals having hydrogenation activity on a carrier in the first stage and a moderately or strongly acidic catalyst comprising one or more metals having hydrogenation activity on a carrier in the second stage.
6. A process according to any one of claims 1-5, characterized in that hydrocracking is carried out as a two-stage process and that the whole reaction product from the first stage is used as the feed for the second stage.
7. A process according to any one of claims 1-6, characterized in that hydrocracking is carried out at an average temperature of from 250 to 4500C, a hydrogen partial pressure of from 25 to 399 bar, a space velocity of from 0.1 to 10 kg.i-l.h-3 and a hydrogen-to-feed ration of from 200 to 3000 Nl.kg- .
8. A process according to any one of claims 1-7, characterized in that the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt is carried out as a two-stage process in the presence of a catalyst consisting of more than 80 tow silica in the first stage and a catalyst comprising one or more metals having hydrogenation activity on a carrier, which carrier consists of more than 40 Yow alumina, in the second stage.
9. A process according to any one of claims 1-8, characterized in that the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt is carried out at an average
**WARNING** end of DESC field may overlap start of CLMS **.
Claims (13)
1. A process for the preparation of one or more atmospheric hydrocarbon oil distillates, characterized in that the preparation is effected, starting from a hydrocarbon oil residue obtained by atmospheric distillation, by catalytic cracking and/or hydrocracking in combination with a catalytic hydrotreatment and deasphalting that the atmospheric residue is subjected to the catalytic hydrotreatment, that the hydrotreated product is separated by distillation into one or more atmospheric distillates, a vacuum distillate and a vacuum residue, that the vacuum residue is separated by deasphalting into a deasphalted oil and asphalt, that the vacuum distillate and the deasphalted oil are converted by catalytic cracking and/or hydrocracking into one or more atmospheric distillates, that at least 50 %w of the asphalt with the hydrocarbon oil residue in a combined feed mixture is again subjected to catalytic hydrotreatment and that the catalytic hydrotreatment is carried out under such conditions that more than 50 Sow of the asphalt present in the feed for the catalytic hydrotreatment is converted into material that does not precipitate in a deasphalting step carried out under the same conditions as the deasphalting of the vacuum residue.
2. A process according to claim 1, characterized in that at least part of the residue obtained in the atmospheric distillation of the catalytically cracked or hydrocracked product is recycled to the cracking unit concerned.
3. A process according to claim 1 or 2, characterized in that catalytic cracking is applied, that part of the residue of the cracked product is recycled to the catalytic cracking unit and/or that a deasphalted oil is used as the feed for the catalytic cracking unit and that these liquids are given a light catalytic hydrotreatment before they are subjected to catalytic cracking.
4. A process according to any one of claims 1-3, characterized in that catalytic cracking is carried out at an average temperature of from 400 to 550"C, a pressure of from 1 to 10 bar, a space velocity of from 0.25 to 4 kg.kg-3.h-3 and a rate of catalyst replenishment of from 0.1 to 5 tonnes of catalyst per 1000 tonnes of feed.
5. A process according to any one of claims 1-4, characterized in that hydrocracking is carried out as a two-stage process in the presence of a weakly or moderately acidic catalyst comprising one or more metals having hydrogenation activity on a carrier in the first stage and a moderately or strongly acidic catalyst comprising one or more metals having hydrogenation activity on a carrier in the second stage.
6. A process according to any one of claims 1-5, characterized in that hydrocracking is carried out as a two-stage process and that the whole reaction product from the first stage is used as the feed for the second stage.
7. A process according to any one of claims 1-6, characterized in that hydrocracking is carried out at an average temperature of from 250 to 4500C, a hydrogen partial pressure of from 25 to 399 bar, a space velocity of from 0.1 to 10 kg.i-l.h-3 and a hydrogen-to-feed ration of from 200 to 3000 Nl.kg- .
8. A process according to any one of claims 1-7, characterized in that the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt is carried out as a two-stage process in the presence of a catalyst consisting of more than 80 tow silica in the first stage and a catalyst comprising one or more metals having hydrogenation activity on a carrier, which carrier consists of more than 40 Yow alumina, in the second stage.
9. A process according to any one of claims 1-8, characterized in that the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt is carried out at an average
temperature of from 375 to 4750C, a hydrogen partial pressure of from 25 to 300 bar, a space velocity of from 0.1 to 3.0 kg.1- .h-l and a hydrogen-to-feed ratio of from 250 to 2500 Nl.kg-l.
10. A process according to any one of claims 1-9, characterized in that the catalytic hydrotreatment of the hydrocarbon oil residue and the asphalt is carried out as a two-stage process and that the first stage is effected in the presence of a quantity of H2S corresponding to an H2S content of the gas at the reactor inlet of more than 10 %v and the second stage in the presence of a quantity of H2S corresponding to an H2S content of the gas at the reactor inlet of less than 5 %v.
11. A process according to any one of claims 1-10, characterized in that both the conversion of the deasphalted oil and the conversion of the vacuum distillate are carried out in the same way, i.e. by either catalytic cracking or hydrocracking, and that these conversions are effected in one unit.
12. A process for the preparation of one or more atmospheric hydrocarbon oil distillates, as claimed in claim 1 substantially as described hereinbefore, with reference to the example.
13. Atmospheric hydrocarbon oil distillates, characterized in that they have been prepared with the aid of a process as claimed in any one or more of claims 1-12.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7612960A NL7612960A (en) | 1976-11-22 | 1976-11-22 | METHOD FOR CONVERTING HYDROCARBONS. |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| GB1560148A true GB1560148A (en) | 1980-01-30 |
Family
ID=19827263
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB4836277A Expired GB1560148A (en) | 1976-11-22 | 1977-11-21 | Process for the conversion of hydrocarbons |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS5364205A (en) |
| CA (1) | CA1117058A (en) |
| DE (1) | DE2751863A1 (en) |
| FR (1) | FR2371504A1 (en) |
| GB (1) | GB1560148A (en) |
| IT (1) | IT1088642B (en) |
| NL (1) | NL7612960A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0082551A1 (en) * | 1981-12-10 | 1983-06-29 | Shell Internationale Researchmaatschappij B.V. | Process for the production of hydrocarbon oil distillates |
| EP0099141A1 (en) * | 1982-07-13 | 1984-01-25 | Shell Internationale Researchmaatschappij B.V. | Process for the production of low-asphaltenes hydrocarbon mixtures |
| GB2148937A (en) * | 1983-11-03 | 1985-06-05 | Chevron Res | Two-stage petroleum residuum hydroconversion using a countercurrent gas-liquid first stage |
| WO2010151300A1 (en) * | 2009-06-23 | 2010-12-29 | Lummus Technology Inc. | Multistage resid hydrocracking |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL190816C (en) * | 1978-07-07 | 1994-09-01 | Shell Int Research | Process for the preparation of gas oil. |
| EP0068543B1 (en) * | 1981-06-25 | 1988-09-21 | Shell Internationale Researchmaatschappij B.V. | Process for the preparation of a hydrocarbon mixture |
| NL8105660A (en) * | 1981-12-16 | 1983-07-18 | Shell Int Research | PROCESS FOR PREPARING HYDROCARBON OIL DISTILLATES |
| JPS58120694A (en) * | 1982-01-13 | 1983-07-18 | Mitsubishi Oil Co Ltd | Preparation of raw material pitch for carbon fiber |
| NL8201233A (en) * | 1982-03-24 | 1983-10-17 | Shell Int Research | PROCESS FOR THE PREPARATION OF LOW ASPHALTENE HYDROCARBON MIXTURE. |
| FR2533228B1 (en) * | 1982-09-17 | 1985-10-11 | Inst Francais Du Petrole | PROCESS FOR CONVERTING A LOAD OF HIGH VISCOSITY HYDROCARBONS INTO A LESS VISCOUS HYDROCARBON FRACTION, MORE EASILY TRANSPORTABLE AND EASIER TO REFIN |
| JPS60152594A (en) * | 1984-01-23 | 1985-08-10 | Kawasaki Heavy Ind Ltd | Desulfurization of residual oil from direct desulphurizer |
| DE3512915A1 (en) * | 1984-04-13 | 1985-10-17 | Deutsche Bp Ag, 2000 Hamburg | Process for the hydroconversion of sulphur-containing heavy hydrocarbons |
| JPS61501855A (en) * | 1984-04-13 | 1986-08-28 | ザ ブリテイツシユ ピトロ−リアム コンパニ− ピ−．エル．シ−． | Hydrogenation conversion method for sulfur-containing heavy hydrocarbons using synthesis gas |
| FR2753982B1 (en) * | 1996-10-02 | 1999-05-28 | Inst Francais Du Petrole | MULTI-STAGE CATALYTIC PROCESS FOR CONVERTING A HEAVY HYDROCARBON FRACTION |
| FR2753984B1 (en) * | 1996-10-02 | 1999-05-28 | Inst Francais Du Petrole | METHOD FOR CONVERTING A HEAVY HYDROCARBON FRACTION INVOLVING HYDRODEMETALLIZATION IN A BUBBLE BED OF CATALYST |
| FR2753983B1 (en) * | 1996-10-02 | 1999-06-04 | Inst Francais Du Petrole | MULTIPLE STEP CONVERSION OF AN OIL RESIDUE |
| CA2862613C (en) * | 2009-12-11 | 2016-02-23 | Uop, Llc | Hydrocarbon composition |
| FR3067037A1 (en) * | 2017-06-02 | 2018-12-07 | IFP Energies Nouvelles | CONVERSION PROCESS COMPRISING FIXED BED HYDROTREATMENT, VACUUM DISTILLATE SEPARATION, VACUUM DISTILLATE HYDROCRACKING STEP |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3168459A (en) * | 1961-05-04 | 1965-02-02 | Sinclair Research Inc | Cracking a metal-contaminated residual oil |
| US3287254A (en) * | 1964-06-03 | 1966-11-22 | Chevron Res | Residual oil conversion process |
| US3905892A (en) * | 1972-03-01 | 1975-09-16 | Cities Service Res & Dev Co | Process for reduction of high sulfur residue |
| US3859199A (en) * | 1973-07-05 | 1975-01-07 | Universal Oil Prod Co | Hydrodesulfurization of asphaltene-containing black oil |
-
1976
- 1976-11-22 NL NL7612960A patent/NL7612960A/en not_active Application Discontinuation
-
1977
- 1977-10-07 CA CA000288341A patent/CA1117058A/en not_active Expired
- 1977-11-21 JP JP13901077A patent/JPS5364205A/en active Granted
- 1977-11-21 IT IT2986877A patent/IT1088642B/en active
- 1977-11-21 GB GB4836277A patent/GB1560148A/en not_active Expired
- 1977-11-21 FR FR7734894A patent/FR2371504A1/en active Granted
- 1977-11-21 DE DE19772751863 patent/DE2751863A1/en active Granted
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0082551A1 (en) * | 1981-12-10 | 1983-06-29 | Shell Internationale Researchmaatschappij B.V. | Process for the production of hydrocarbon oil distillates |
| EP0099141A1 (en) * | 1982-07-13 | 1984-01-25 | Shell Internationale Researchmaatschappij B.V. | Process for the production of low-asphaltenes hydrocarbon mixtures |
| GB2148937A (en) * | 1983-11-03 | 1985-06-05 | Chevron Res | Two-stage petroleum residuum hydroconversion using a countercurrent gas-liquid first stage |
| WO2010151300A1 (en) * | 2009-06-23 | 2010-12-29 | Lummus Technology Inc. | Multistage resid hydrocracking |
| US8287720B2 (en) | 2009-06-23 | 2012-10-16 | Lummus Technology Inc. | Multistage resid hydrocracking |
| EP2562235A1 (en) * | 2009-06-23 | 2013-02-27 | Lummus Technology Inc. | Multistage resid hydrocracking |
| RU2495911C2 (en) * | 2009-06-23 | 2013-10-20 | Ламмус Текнолоджи Инк. | Multistage hydrocracking of refining residues |
| RU2538961C1 (en) * | 2009-06-23 | 2015-01-10 | Ламмус Текнолоджи Инк. | Multi-stage hydrocracking of distillation residues |
| US9441174B2 (en) | 2009-06-23 | 2016-09-13 | Lummus Technology Inc. | Multistage resid hydrocracking |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5364205A (en) | 1978-06-08 |
| IT1088642B (en) | 1985-06-10 |
| JPS618120B2 (en) | 1986-03-12 |
| FR2371504A1 (en) | 1978-06-16 |
| DE2751863C2 (en) | 1989-11-02 |
| DE2751863A1 (en) | 1978-05-24 |
| FR2371504B1 (en) | 1982-12-10 |
| NL7612960A (en) | 1978-05-24 |
| CA1117058A (en) | 1982-01-26 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PS | Patent sealed | ||
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19921121 |