CA1206906A - Process for the production of deasphalted oils and hydrocarbon distillates - Google Patents
Process for the production of deasphalted oils and hydrocarbon distillatesInfo
- Publication number
- CA1206906A CA1206906A CA000423215A CA423215A CA1206906A CA 1206906 A CA1206906 A CA 1206906A CA 000423215 A CA000423215 A CA 000423215A CA 423215 A CA423215 A CA 423215A CA 1206906 A CA1206906 A CA 1206906A
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- Prior art keywords
- feed
- stream
- treatment
- asphaltenes
- fraction
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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
- 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
- C10G69/06—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 thermal cracking in the absence of hydrogen
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (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)
- Polymers With Sulfur, Phosphorus Or Metals In The Main Chain (AREA)
Abstract
A B S T R A C T
PROCESS FOR THE PRODUCTION OF DEASPHALTED OILS
AND HYDROCARBON OIL DISTILLATES
Deasphalted oils and distillates are produced from as-phaltenes-rich hydrocarbon mixtures by a process comprising subject mg the feed to thermal cracking and subjecting the re-sulting heavy fraction to a combination of a catalytic hydro-treatment and a solvent deasphalting.
PROCESS FOR THE PRODUCTION OF DEASPHALTED OILS
AND HYDROCARBON OIL DISTILLATES
Deasphalted oils and distillates are produced from as-phaltenes-rich hydrocarbon mixtures by a process comprising subject mg the feed to thermal cracking and subjecting the re-sulting heavy fraction to a combination of a catalytic hydro-treatment and a solvent deasphalting.
Description
9~i PK)CESS EOR THE PFODUCTION OF DE~SPH~ D OILS
AND HYDK)C~ON OIL DISTILL~ES
The invention relates to a process for the production of deasphalted oils and hydrocarbon oil distillates frcm asphaltenes-containing hydrocarbon mixtures.
The atmospheric distillation of crude mineral oil for the production of light hydrocarbon oil distillates, such as gasoline, kerosine and gas oil yields an asphaltenes-containing residue as a by-product. Originally these residues (which usually in addition to asphaltenes also contain a considerable percentage of sulphur and m tals) were used as fuel oil. In view of the growing demand of light hydrocarbon oil distillates and the shrinking reserves of crude mlneral oil, several treatments aiming at the production of light hydrocarbon oil distillates frcm atmospheric residues have already been proposed~ For instance, a deasphalted oil may be separated from an atmospheric residue by solvent deasphalting and this deasphalted oil may be subjected to catalytic cracking in the presence or absence of hydrogen. Another option is to separate an a~,vspheric residue into a vacuum distillate and a vacuum residue by vacuum distillation, to separate a deasphalted oil from the vacuum residue by solvent deasphalting and to subject both the vacuum distillate and the deasphalted oil to catalytic cracking in the presence or absence of hydrogen.
Solvent deasphalting (D~), a process in which an asphaltenes-containing feedstock is converted into a product from which a deasphalted oil can be separated as the desired main prod~ct and an asphaltic bitumen as a by-product, has proven in actual prac-tice to be a suitable treabment for the production of deasphalted oils from a variety of asphaltenes-containing hydroc æbon mux-tures.
It has now been investigated whether combining the DA treat-ment with a pretreatment of the asphaltenes-containing feed and/or ~'K3 .~Sp,`~
~2~6~6 an aftertreatment of the asphaltic bitumen separated in the DA
treatment and using at least part of the asphaltic bitumen that has been subjected to the aftertreatment as the feed for the DA, might yield better results than employing nothing but the DA. In the assessment of the results the yields of deasphalted oil and ligh~ product(s) are most important. The qualities of the de-asphalted oil and the light product(s~ as well as the quality of the heavy by-product are also important. In this context the quality of the deasphalted oil is taken to be its suitability for conversion into hydrocarbon oil distillates by catalytic cracking in the presence or absence of hydrogenO This suitability is greater according as the deasphalted oil has, among other things, lower asphaltenes, metal and sulphur contents. In this context the quality of the light product is taken to be its suitability for processing into a valuable light fuel. This suitability is greater according as the light product has, among other things, lower sulphur and olefins contents. In this context the quality of the heavy product is taken to ~e its suitability for serving as a fuel oil component. This suitability is greater according as the heavy product has, among other things, lower metal and sulphur contents and lower viscosity and density. For use as pretreatments of ~he feed for the DA and as aftertreatments of the asphaltic bitumen separated in the DA, the following treatments were investigated:
thermal cracking (TC) in which a heavy feed is converted into a product which contains less than 20 %w C4 hydrocarbons and from which one or more distillate fractions and a heavy fraction are separated and catalytic hydrotreatment (HT) in which an as-phaltenes-containing feed is converted into a product having a reduced asphaltenes content fm m which one or more distillate 3 fractions and a heavy fraction are separated~
During this investigation a ccmparison was made between the results that can be obtained when a deasphalted oil and possibly a hydrocarbon oil distillate having a given boiling range as well as a heavy by-product are produced starting from equal quantities of S~06 an asphaltenes-containing hydrocarbon mixture by using a) DA only, b) DA in ccmbination with TC, c) DA in ccmbination with HT and d) DA in ccmbination with both TC and HT, the conditions of the various treatments beiny similar as much as possible. In view of quantity and quality of the deasphalted oil and the hydrocarbon oil distillate to be obtained in each of the procedures and the quality of the heavy by-product, the various procedures may be arranged as follows:
Quantity of deasphalted oil d = c > b = a 10 Quality of the deasphalted oil d = c > b = a Quantity of hydrocarbon oil distillate d > c > b Quality of the hydrocarbon oil distillate c > d > b Quality of the heavy product c ~ d ~ a ~ b Taking into account the considerable difference in hydro-carbon oil distillate yields obtained according to procedures c) and d) and the no more than minor differences in quality between the hydrocarbon oil distillates and between the heavy by-products obtained according to procedures c) and d) a procedure in which a combination is used of a DA treatment~ a TC treatment and a HT, is much preferred.
As regards the order in which the three treatments æ e carried out, a number of embodim~nts may be considered. Each of the embidime~ts may be placed in one of the two following classes.
I. The asphaltenes-containing feed is first subjected to a HT or a DA treatment and the heavy fraction or asphaltic bitumen separated from the respective products obtained is subjected to a combination of a DA treatment and a TC treatment or a co~bination of a TC treatment and a HT, respectively.
II. The asphaltenes-containing feed is first subjected to a TC
treatment and the heavy fraction separated from the product obtained is subjected to a ccmbination of a DA treatment and a HT.
The embodiments belonging to class II constitute the subject matter of the present patent application.
l .
1;~6906 m e embodiments to which the present patent application relates, may be subdivided further depending on whether the heavy fraction separated frcm the product of the TC treatment is used as feed or feed ccmponent for the HT (class IIA) or as feed or feed component for the DA treatment (class IIB). In the ~mbodlments be-longing to class IIA the heavy fraction separated from the product of the HT is used as the feed for the DA treatment. In the embodi-ments belonging to class IIB the asphaltic bitumen fraction is used as the feed for the HT and the heavy fraction separated from the product of the ~T is used as a feed component for the TC
treatment and/or as a feed component for the DA treatment.
m e present patent application therefore relates to a process for the production of deasphalted oils and hydrocarbon oil distil-lates from asphaltenes-containing hydrocarbon mixtures, in which an asphaltenes-containing hydrocarbon mLxture ~stream l) is subjected to a thermal cracking treatment (TC) in which a feed is converted into a product which contains less than 20 %w C4 hydroc æ~ons and from which one or more distillate fractions and a heavy fraction (stream 4) are separated, in which stream 4 is subjected to a ccmbination of the following two treatments: a catalytic hydrotreatment (HT) in which an asphaltenes-containing feed is converted into a product which has a reduced asphaltenes content and from which one or more distillate fractions and a heavy fraction (~tream 2) are separated and a solvent deasphalting treatment (DA) in which an asphaltenes-containing feed is con-verted into a product from which a deasphalted oil fraction and an asphaltic bitumen fraction (stream 3) are separated, and in which stream 4 is used either 1) as feed or feed component for the HT with stream 2 being used as the feed for the DA treatment, or
AND HYDK)C~ON OIL DISTILL~ES
The invention relates to a process for the production of deasphalted oils and hydrocarbon oil distillates frcm asphaltenes-containing hydrocarbon mixtures.
The atmospheric distillation of crude mineral oil for the production of light hydrocarbon oil distillates, such as gasoline, kerosine and gas oil yields an asphaltenes-containing residue as a by-product. Originally these residues (which usually in addition to asphaltenes also contain a considerable percentage of sulphur and m tals) were used as fuel oil. In view of the growing demand of light hydrocarbon oil distillates and the shrinking reserves of crude mlneral oil, several treatments aiming at the production of light hydrocarbon oil distillates frcm atmospheric residues have already been proposed~ For instance, a deasphalted oil may be separated from an atmospheric residue by solvent deasphalting and this deasphalted oil may be subjected to catalytic cracking in the presence or absence of hydrogen. Another option is to separate an a~,vspheric residue into a vacuum distillate and a vacuum residue by vacuum distillation, to separate a deasphalted oil from the vacuum residue by solvent deasphalting and to subject both the vacuum distillate and the deasphalted oil to catalytic cracking in the presence or absence of hydrogen.
Solvent deasphalting (D~), a process in which an asphaltenes-containing feedstock is converted into a product from which a deasphalted oil can be separated as the desired main prod~ct and an asphaltic bitumen as a by-product, has proven in actual prac-tice to be a suitable treabment for the production of deasphalted oils from a variety of asphaltenes-containing hydroc æbon mux-tures.
It has now been investigated whether combining the DA treat-ment with a pretreatment of the asphaltenes-containing feed and/or ~'K3 .~Sp,`~
~2~6~6 an aftertreatment of the asphaltic bitumen separated in the DA
treatment and using at least part of the asphaltic bitumen that has been subjected to the aftertreatment as the feed for the DA, might yield better results than employing nothing but the DA. In the assessment of the results the yields of deasphalted oil and ligh~ product(s) are most important. The qualities of the de-asphalted oil and the light product(s~ as well as the quality of the heavy by-product are also important. In this context the quality of the deasphalted oil is taken to be its suitability for conversion into hydrocarbon oil distillates by catalytic cracking in the presence or absence of hydrogenO This suitability is greater according as the deasphalted oil has, among other things, lower asphaltenes, metal and sulphur contents. In this context the quality of the light product is taken to be its suitability for processing into a valuable light fuel. This suitability is greater according as the light product has, among other things, lower sulphur and olefins contents. In this context the quality of the heavy product is taken to ~e its suitability for serving as a fuel oil component. This suitability is greater according as the heavy product has, among other things, lower metal and sulphur contents and lower viscosity and density. For use as pretreatments of ~he feed for the DA and as aftertreatments of the asphaltic bitumen separated in the DA, the following treatments were investigated:
thermal cracking (TC) in which a heavy feed is converted into a product which contains less than 20 %w C4 hydrocarbons and from which one or more distillate fractions and a heavy fraction are separated and catalytic hydrotreatment (HT) in which an as-phaltenes-containing feed is converted into a product having a reduced asphaltenes content fm m which one or more distillate 3 fractions and a heavy fraction are separated~
During this investigation a ccmparison was made between the results that can be obtained when a deasphalted oil and possibly a hydrocarbon oil distillate having a given boiling range as well as a heavy by-product are produced starting from equal quantities of S~06 an asphaltenes-containing hydrocarbon mixture by using a) DA only, b) DA in ccmbination with TC, c) DA in ccmbination with HT and d) DA in ccmbination with both TC and HT, the conditions of the various treatments beiny similar as much as possible. In view of quantity and quality of the deasphalted oil and the hydrocarbon oil distillate to be obtained in each of the procedures and the quality of the heavy by-product, the various procedures may be arranged as follows:
Quantity of deasphalted oil d = c > b = a 10 Quality of the deasphalted oil d = c > b = a Quantity of hydrocarbon oil distillate d > c > b Quality of the hydrocarbon oil distillate c > d > b Quality of the heavy product c ~ d ~ a ~ b Taking into account the considerable difference in hydro-carbon oil distillate yields obtained according to procedures c) and d) and the no more than minor differences in quality between the hydrocarbon oil distillates and between the heavy by-products obtained according to procedures c) and d) a procedure in which a combination is used of a DA treatment~ a TC treatment and a HT, is much preferred.
As regards the order in which the three treatments æ e carried out, a number of embodim~nts may be considered. Each of the embidime~ts may be placed in one of the two following classes.
I. The asphaltenes-containing feed is first subjected to a HT or a DA treatment and the heavy fraction or asphaltic bitumen separated from the respective products obtained is subjected to a combination of a DA treatment and a TC treatment or a co~bination of a TC treatment and a HT, respectively.
II. The asphaltenes-containing feed is first subjected to a TC
treatment and the heavy fraction separated from the product obtained is subjected to a ccmbination of a DA treatment and a HT.
The embodiments belonging to class II constitute the subject matter of the present patent application.
l .
1;~6906 m e embodiments to which the present patent application relates, may be subdivided further depending on whether the heavy fraction separated frcm the product of the TC treatment is used as feed or feed ccmponent for the HT (class IIA) or as feed or feed component for the DA treatment (class IIB). In the ~mbodlments be-longing to class IIA the heavy fraction separated from the product of the HT is used as the feed for the DA treatment. In the embodi-ments belonging to class IIB the asphaltic bitumen fraction is used as the feed for the HT and the heavy fraction separated from the product of the ~T is used as a feed component for the TC
treatment and/or as a feed component for the DA treatment.
m e present patent application therefore relates to a process for the production of deasphalted oils and hydrocarbon oil distil-lates from asphaltenes-containing hydrocarbon mixtures, in which an asphaltenes-containing hydrocarbon mLxture ~stream l) is subjected to a thermal cracking treatment (TC) in which a feed is converted into a product which contains less than 20 %w C4 hydroc æ~ons and from which one or more distillate fractions and a heavy fraction (stream 4) are separated, in which stream 4 is subjected to a ccmbination of the following two treatments: a catalytic hydrotreatment (HT) in which an asphaltenes-containing feed is converted into a product which has a reduced asphaltenes content and from which one or more distillate fractions and a heavy fraction (~tream 2) are separated and a solvent deasphalting treatment (DA) in which an asphaltenes-containing feed is con-verted into a product from which a deasphalted oil fraction and an asphaltic bitumen fraction (stream 3) are separated, and in which stream 4 is used either 1) as feed or feed component for the HT with stream 2 being used as the feed for the DA treatment, or
2) as feed or feed component for the DA treatment with stream 3 being used as the feed for the HT and stream 2 as a feed comr ponent for the TC treatment and/or as a feed component for the DA treatment.
i In the process according to the invention the feed used is an asphaltenes-containing hydrocarbon mixture. A suitable parameter for the assessment of the asphaltenes content of a hydroc æbon muxture as well as of the reduction of the asphaltenes content which appears when an asphaltenes-containing hydrocarbon mixture is subjected to a HT, is the Ramsbottom Carbon Test value (RCT).
The higher the asphaltenes content of the hydrocarbon mlxture, the higher the RCT. Preferably, the process is applied to hydrocarbon mlxtures which boil substantially above 350C and more than 35 ~w of which boils above 520C and which have an RCT higher than 7.5 %w. Examples of such hydrocarbon mixtures are residues obtained in the distillation of crude mineral oils and also heavy hydrocarb~n mlxtures obtained frcm shale and tar sands. If required, the process may also be applied to heavy crude mineral oils, residues obtained in the distillation of products formed in the thermal cracking of hydrocarbon moxtures and asphaltic bitumen obtained in the solvent deasphalting of asphaltenes-containing hydrocæbon mixtures. m e process according to the invention can very suitably be applied to residues obtained in the vacuum distillation of atmospheric distillation residues from crude mineral oils. If an atmospheric distillation residue from a crude mlneral oil is available as feed for the process according to the invention, it is preferred to separate a vacuum distillate therefram by vacuum distillation and to subject the resulting vacuum residue to the TC
treatment. The separated vacuum distillate may be subjected to thermal crack m g or to catalytic cracking in the presence or in the absence of hydrogen to convert it into light hydrocarbon oil distillates.
The process according to the invention is a three-step
i In the process according to the invention the feed used is an asphaltenes-containing hydrocarbon mixture. A suitable parameter for the assessment of the asphaltenes content of a hydroc æbon muxture as well as of the reduction of the asphaltenes content which appears when an asphaltenes-containing hydrocarbon mixture is subjected to a HT, is the Ramsbottom Carbon Test value (RCT).
The higher the asphaltenes content of the hydrocarbon mlxture, the higher the RCT. Preferably, the process is applied to hydrocarbon mlxtures which boil substantially above 350C and more than 35 ~w of which boils above 520C and which have an RCT higher than 7.5 %w. Examples of such hydrocarbon mixtures are residues obtained in the distillation of crude mineral oils and also heavy hydrocarb~n mlxtures obtained frcm shale and tar sands. If required, the process may also be applied to heavy crude mineral oils, residues obtained in the distillation of products formed in the thermal cracking of hydrocarbon moxtures and asphaltic bitumen obtained in the solvent deasphalting of asphaltenes-containing hydrocæbon mixtures. m e process according to the invention can very suitably be applied to residues obtained in the vacuum distillation of atmospheric distillation residues from crude mineral oils. If an atmospheric distillation residue from a crude mlneral oil is available as feed for the process according to the invention, it is preferred to separate a vacuum distillate therefram by vacuum distillation and to subject the resulting vacuum residue to the TC
treatment. The separated vacuum distillate may be subjected to thermal crack m g or to catalytic cracking in the presence or in the absence of hydrogen to convert it into light hydrocarbon oil distillates.
The process according to the invention is a three-step
3 process in which in the first step an asphaltenes-containing feed (stream 1) is subjected to a TC treatment for the production of a product which contains less than 20 ~w C4 hydrocarbons and from which one or more distillate fractions and a heavy fraction lZC~6906 (stream 4) are separated. In the second and third steps of the process stream 4 is subjected to a ccmbination of a DA treatment and a HT. m e distillate fractions separated from the product of the TC treatment may be atmospheric distillates only, but pre-ferably a vacuum distillate should be separated from the product aswell. m is vacuum distilla~e may be converted into light hydro-carbon oil distillates in the ways indicated hereinbefore. The TC
treatment is preferably carried out at a temperature of from 400-525C and a space velocity of from 0.01-5 kg fresh feed per litre cracking reactor volume per minute.
In the process according to the invention the second or third step used is a ET in which an asphaltenes~containing feed is converted into a product which has a reduced asphaltenes con~ent and fram which one or m~re distillate fractions and a heavy fraction (stream 2) are separated.
Asphaltenes-containing hydrocarbon mixtures usually include a considerable percentage of metals, particularly vanadium and nickel. When such hydrocarbon mixtures are subjected to a cata-lytic treatment, for instance a H~ for the reduction of the asphaltenes content as is the case in the process according to the invention, these metals are deposited on the catalyst used in the HT and thus shorten its effective life. In view of this, as-phaltenes-containing hydrocarbon mlxtures having a vanadium +
nickel content of more than 50 parts per million by weight (ppmw) should preferably be subjected to a demetallization treatment before they are contacted with the catalyst used in the HT. m is demetallization may very suitably be carried out by contacting the asphaltenes-containing hydrocarbon mixture, in the presence of hydrogen, with a catalyst consisting more than 80 %w of silica.
Both catalysts consisting entirely of silica and catalysts con-taining one or more metals having hydrogenating activity - in particular a ccmbination of nickel and vanadium - emplaced on a carrier substantially consisting of silica, are suitable for the purpose. When in the process according to the invention an as-phaltenes-containing feed is sub~ected to a catalytic demetal-lZ06g~6 lization treatment in the presence of hydrogen, this demetal-lization may be carried out in a separate reactor. Since the catalytic demetallization and the HT for the reduction of the asphaltenes content can be carried out under the same conditions, the two processes may very suitably be carried out in the same reactor containing a bed of the demetallization catalyst and a bed of the catalyst used in the HT, successively.
Suitable catalysts for carrying out the HT are those con-taining at least one metal chosen frcm the group formed by nickel and cobalt and in addition at least one metal chosen from the group formed by molybdenum and tungsten on a carrier, which carrier consists more than 40 %w of alumina. Catalysts very suitable for use in the HT are those comprising the metal combi-nations nickel/molybdenum or cobalt/molybdenum on alumina as the carrier. The HT is preferably carried out at a temperature of from 300-500C and in particular of from 350-450C, a pressure of frcm 50-300 bar and in particular of from 75-200 bar, a space velocity of from 0.02-10 g.g l.h 1 and in particular of from 0.1-2 g.g l.h 1 and a H2/feed ratio of from 100-5000 Nl.kg 1 and in particular of from 500~2000 Nl.kg 1. The conditions used in a catalytic demetallization treatment in the presence of hydrogen, to be carried out if required, are subject to the same preference as those for the ~T for the reduction of the asphaltenes content stated hereinbefore.
The HT is preferably carried out in such a way that it yields a product, the C5+ fraction of which meets the following requirements:
a) the RCT of the C5 fraction amcunts to 20-70% of the RCT of the feed, and b) the difference between the percentages by weight of hydro-carbons boiling below 350C present in the C5+ fraction and in the feed is at most 40.
It should be noted that in the catalytic demetallization the reduction of the metal content is accompanied by some reduction of ~2069(~6 the RCT and same formation of C5-350C product. A similar phenomenon occurs in the HT, in which the reduction of the RfT and formation of C5-350C product are accompanied by some reduction of the metal content. The requirements mentioned under a) and b) refer to the total RCT reduction and the total formation of C5-350C
product (viz. including those occurring in a catalytic demetal-lization treatment that may be carried out).
The HT yields a product having a reduced asphaltenes content from which one or m~re distillate fractions and a heavy fraction (stream 2~ are separated. m e distillate fractions separated from the product may be atmospheric distillates only, but it is pre-ferred to separate a vacuum distillate from the product as well.
This vacuum distillate may be converted into light hydrocarbon oil distillates in the ways stated here mbefore.
In the process according to the invention the ~econd or third step used is a DA treatment in which an asphaltenes-containing feed is converted into a product fram which a deasphalted oil and an asphaltic bitumen (stream 3) are separated. Suitable solvents for carry mg out the DA treatment are paraffinic hydrocarbons having 3~6 carbon atoms per molecule, such as n-butane and mix-tures thereof, such as n ~ tures of propane and n-butane and mixtures of n-butane and n-pentane. Suitable solvent/oil weight ratios lie between 7.1 and 1:1 and in particular between 4:1 and 1:1. m e DA treatment is preferably carried out at a pressure in the range of between 20 and 100 bar. When n-butane is used as the sol-vent, the deasphalting is preferably carried out at a pressure of from 35-45 bar and a temperature of frcm 100-150C.
As noted hereinbefore, a subdivision of the embodiments belonging to class II, to which the present patent application 3o relates, may be made depending on whether stream 4 is used as feed or feed oomponent for the HT (class II~) or as feed or feed component for the DA treatment (class IIB). In the embodiments belonging to class IIA stream 2 is used as the feed for the 12069~
DA treatment. In the embodiments ~elonging to class IIB stream 3 is used as the feed for the ~T and stream 2 is used as a feed component for the TC treatment and/or as a feed component for the DA treatment.
m e various embod~ments belonging to class IIA are repre-sented schematically in Figure I. m e various streams, fractions and reaction zones are indicated by three digit numbers, the first of which refers to the Figure concerned. The vacuum residue (302~, for instance, refers to vacuum residue 2 in the context of Figure III. According to Figure I the process is carried out in an ap-paratus ccmprising a TC zone (lOS), a HT zone (106) and a DA zone (107), successively. An asphaltenes-containing hydrocarbon mixture (101) is subjected to a TC treatment and the cracked product is separated into one or more distillate fractions (108) and a resi-dual fraction (104). Stream 4 is subjected to a HT and the hydro-treated product is separated into one or more distillate fractions (109) and a residual fraction (102). Stream 2 is subjected to a DA
treatment and the product is separated into a deasphalted oil (110) and an asphaltic bitumen (103). In addition to this embodi-ment(IIA1), in which stream 103 is subjected to no further treat-ment, Figure I includes the follcwing three embodinents:
II~2 The use of at least part of stre~m 103 as a feed component for the TC treatment.
IIA3 The use of at least part of stream 103 as a feed component for the HT.
IIA4 The use of part of stream 103 as a feed component for the TC treatment and as a feed component for the HT.
12o69~6 m e various embodiments belonging to class IIB are repre-sented schematically in Figure II. According to this Figure the process is carried out in an apparatus comprising a TC zone (205), a DA zone (206) and a HT zone (207), successively. An asphaltenes-containing hydrocarbon mixture (201) is subjected to a TC treat-ment and the cracked product is separated into one or more dis-tillate fractions (208) and a residual fraction (204). Stream 204 is subjected to a DA treatment and the product is separated into a deasphalted oil (209) and an asphaltic bitumen (203). Stream 203 is subjected to a HT and the hydrotreated product is separated into one or more distillate fractions (210) and a residual frac-tion (202). Stream 202 is used either as a feed component for the TC treatment (embodiment IIBl) or as a feed CQmpOnent for the DA
treatment (embodiment IIB2) or as a feed component both for the TC
treatment and for the DA treatment (~nbodlTent IIB33.
In the embodiments aiming at the completest possible con-version of stream (.01) into deasphalted oil and hydrocarbon oil distillates, what is called a l'bleed stream" should preferably be separated f m m one of the heavy streams of the process. In that way the build-up during the process of undesirably heavy CQmpC-nents can be obviated.
Two flcw diagrams for the preparatio~ of deasphalted oil and hydrocar~on oil distillates from asphaltenes-containing hydro-carbon mixtures according to the invention will hereinafter be elucidated in more detail with the aid of Figures III and IV.
Flow diagLram A (based on embodiment IIB2) See Figure III.
The process is carried out in an apparatus comprising a TC zone composed of a thermal cracking unit ~305), an atmospheric dis-tillation unit (306) and a vacuum distillation unit (307), suc-cessively, a HT zone composed of a unit for catalytic hydro-treatment (308), a second atmospheric distillation unit (309) and a second vacuum distillation unit (310) and a DA zone t311). An asphaltenes-containing hydrocarbon mixture (301) is muxed with an asphaltic bitumen stream (312) and the mixture (313) is subjected to thermal cracking. m e cracked product (314) is separated by atmospheric distillation into a gas fraction (315), an atmospheric distillate (316) and an atmospheric residue (317). The atmospheric residue (317) is separated by vacuum distillation into a vacuum distillate (318) and a vacuum residue (304). The vacuum residue (304) is subjected together with hydrogen (319) to catalytic hydrotreatment. The hydrotreated product (320) is separated by atm~spheric distillation into a gas fraction (321), an atmospheric distillate (322) and an a~,~spheric residue (323). m e atm~spheric residue (323) is separated by vacuum distillation into a vacuum distillate (324) and a vacuum residue (302). The vacuum residue (302) is separated by solvent deasphalting into a deasphalted oil (325) and an asphaltic bitumen (303). The asphaltic bitumen (303) is divided into two portions (312) and (326).
Flow diaqram B (based on embodinent IIB1) See Figure IV.
The process is carried out in an apparatus compris m g a TC zone composed of a thermal cracking unit 1405), an atmospheric dis-tillation unit (406) and a vacuum distillation unit (407), suc-cessively, a DA zone (408) and a HT zone ccmposed of a unit for catalytic hydrotreatment (409), a second atmospheric dis-tillation unit (410) and a second vacuum distillation unit (411).
An asphaltenes-containing hydrocarbon muxture (401) is mixed with a vacuum residue (402) and the mixture 1412) is subjected to thermal cracking. The cracked product (413) is separated by atm~spheric distillation into a gas fraction (414), an atmospheric distillate (415) and an atmospheric residue (416). The atmospheric residue (416) is separated by vacuum distillation into a vacuum 12069t~6 distillate (417) and a vacuum residue (418). The vacuum residue (418) is separated by solvent deasphalting into a deasphalted oil (419) and an asphaltic bitumen (403). m e asphaltic bitumen (403) is divided into two portions (420) and (421). Portion (421) is subjected together with hydrogen (422) to catalytic hydrotreat-ment. m e hydrotreated product (423) is separated by atmospheric distillation into a gas fraction ~424), an atmospheric distillate (425) and an atmospheric residue (426~. m e atmospheric residue (426) is separated by vacuum distillation into a vacuum distillate (427) and a vacuum residue ~402).
The present patent application also includes apparatuses for carrying out the process according ~o the invention, which cor-respond substantially with those represented schematically by Figures I- IV.
The invention is now elucidated with the aid of the following Examples.
In the process according to the i~vention two asphaltenes-containing hydrocarbon mixtures obtained as residues in the vacuum distillation of atmospheric distillation residues frcm cxude mineral oils were used as the starting material. The vacuum residues both boiled substantially above 520C and they had RfT's of 18.2 and 12.3 %w. The process according to the invention was carried out according to flow diagrams A and B. The conditions used in the various zones were the follcwing.
In both the flcw diagrams the units for catalytic hydrotreat-ment consisted of two reactors, the first of which was filled with a Ni/V/SiO2 catalyst conta:ining 0.5 parts by weight (pbw) nickel and 2.0 pbw vanadium per 100 pbw silica and the second of which was filled with a Co/Mo/A1203 catalyst containing 4 pbw cobalt and 12 pbw moly~denum per 100 pbw alumina. The catalysts were used in a 1:4 volume ratio. The catalytic hydrotreatment was carried out at a hydrogen pressure of 150 bar, a space velocity (measured 3~2~906 over the two reactors) of 0.5 kg feed per litre catalyst per hour, a H2/feed ratio of 1000 Nl per kg and an average temperature of 410C in the first reactor and of 385C in the second reactor.
In both the flow diagrams the DA treatment was carried out using n-butane as the solvent, at a temperature of 115C, a pressure of 40 bar and a solvent/oil weight ratio of 3:1.
In both the flow diagrams the ~C treatment was carried out in a cracking coil at a pressure of 10 bar, a space velocity of 0.4 kg fresh feed per litre cracking coil volume per minute and a temperature of 485C (t~mperature measured at the outlet of the cracking coil).
Example 1 This Example was carried out according to flow diagr~m A as represented by Figure III.
100 pbw vacuum residue (301) having an R~T of 18.2 %w yielded the various streams in the following quantities:
115.8 pkw muxture (313), 15.0 " C5-350C atmospheric distillate (316), 98.6 " 350C~ atmospheric residue (317), 11.8 " 350-520C vacuum distillate (318), 86.8 " 520C+ vacuum residue (304) having an R~T of 34.6 ~w, a product (320), the C5 fraction of which had an RCT of 15.9 %w, 11.6 pbw C5-350C atmospheric distillate (322), 71.3 " 350C atmospheric residue (323), 17.4 " 350-520C vacuum distillate (324), 53.9 1l 520C~ vacuum residue (302), 29.1 " deasphalted oil (325), 24.8 " asphaltic bitumen (303), 15.8 " portion (312) and 9.0 " portion (326).
Example 2 This Example was carried out according to flow diagram B as represented by Figure IV.
100 pbw vacuum residue (401) having an RCT of 12.3 %w yielded ~2069~6 _he various streams in the following ~uantities:
113.1 pbw muxture (412), 18.8 " C5-350C atmDspheric distillate (415), 91.6 " 350C+ atm~spheric residue (416), 14.7 " 350-520C vacuum distillate (417~, 76.9 " 520C~ vacuwm residue (418), 46.1 " deasphalted oil (419~, 30.8 " asphaltic bitumen (403), 8.6 " portion (4203, 22.2 " portion (421) having an RCT of 50.0 ~w, a product (423), the C5 fraction of which had an RCT of 27.5 %w, 3.2 pbw C5-350C atm~spheric distillate (425), 17.9 " 350C+ atmospheric residue (426),
treatment is preferably carried out at a temperature of from 400-525C and a space velocity of from 0.01-5 kg fresh feed per litre cracking reactor volume per minute.
In the process according to the invention the second or third step used is a ET in which an asphaltenes~containing feed is converted into a product which has a reduced asphaltenes con~ent and fram which one or m~re distillate fractions and a heavy fraction (stream 2) are separated.
Asphaltenes-containing hydrocarbon mixtures usually include a considerable percentage of metals, particularly vanadium and nickel. When such hydrocarbon mixtures are subjected to a cata-lytic treatment, for instance a H~ for the reduction of the asphaltenes content as is the case in the process according to the invention, these metals are deposited on the catalyst used in the HT and thus shorten its effective life. In view of this, as-phaltenes-containing hydrocarbon mlxtures having a vanadium +
nickel content of more than 50 parts per million by weight (ppmw) should preferably be subjected to a demetallization treatment before they are contacted with the catalyst used in the HT. m is demetallization may very suitably be carried out by contacting the asphaltenes-containing hydrocarbon mixture, in the presence of hydrogen, with a catalyst consisting more than 80 %w of silica.
Both catalysts consisting entirely of silica and catalysts con-taining one or more metals having hydrogenating activity - in particular a ccmbination of nickel and vanadium - emplaced on a carrier substantially consisting of silica, are suitable for the purpose. When in the process according to the invention an as-phaltenes-containing feed is sub~ected to a catalytic demetal-lZ06g~6 lization treatment in the presence of hydrogen, this demetal-lization may be carried out in a separate reactor. Since the catalytic demetallization and the HT for the reduction of the asphaltenes content can be carried out under the same conditions, the two processes may very suitably be carried out in the same reactor containing a bed of the demetallization catalyst and a bed of the catalyst used in the HT, successively.
Suitable catalysts for carrying out the HT are those con-taining at least one metal chosen frcm the group formed by nickel and cobalt and in addition at least one metal chosen from the group formed by molybdenum and tungsten on a carrier, which carrier consists more than 40 %w of alumina. Catalysts very suitable for use in the HT are those comprising the metal combi-nations nickel/molybdenum or cobalt/molybdenum on alumina as the carrier. The HT is preferably carried out at a temperature of from 300-500C and in particular of from 350-450C, a pressure of frcm 50-300 bar and in particular of from 75-200 bar, a space velocity of from 0.02-10 g.g l.h 1 and in particular of from 0.1-2 g.g l.h 1 and a H2/feed ratio of from 100-5000 Nl.kg 1 and in particular of from 500~2000 Nl.kg 1. The conditions used in a catalytic demetallization treatment in the presence of hydrogen, to be carried out if required, are subject to the same preference as those for the ~T for the reduction of the asphaltenes content stated hereinbefore.
The HT is preferably carried out in such a way that it yields a product, the C5+ fraction of which meets the following requirements:
a) the RCT of the C5 fraction amcunts to 20-70% of the RCT of the feed, and b) the difference between the percentages by weight of hydro-carbons boiling below 350C present in the C5+ fraction and in the feed is at most 40.
It should be noted that in the catalytic demetallization the reduction of the metal content is accompanied by some reduction of ~2069(~6 the RCT and same formation of C5-350C product. A similar phenomenon occurs in the HT, in which the reduction of the RfT and formation of C5-350C product are accompanied by some reduction of the metal content. The requirements mentioned under a) and b) refer to the total RCT reduction and the total formation of C5-350C
product (viz. including those occurring in a catalytic demetal-lization treatment that may be carried out).
The HT yields a product having a reduced asphaltenes content from which one or m~re distillate fractions and a heavy fraction (stream 2~ are separated. m e distillate fractions separated from the product may be atmospheric distillates only, but it is pre-ferred to separate a vacuum distillate from the product as well.
This vacuum distillate may be converted into light hydrocarbon oil distillates in the ways stated here mbefore.
In the process according to the invention the ~econd or third step used is a DA treatment in which an asphaltenes-containing feed is converted into a product fram which a deasphalted oil and an asphaltic bitumen (stream 3) are separated. Suitable solvents for carry mg out the DA treatment are paraffinic hydrocarbons having 3~6 carbon atoms per molecule, such as n-butane and mix-tures thereof, such as n ~ tures of propane and n-butane and mixtures of n-butane and n-pentane. Suitable solvent/oil weight ratios lie between 7.1 and 1:1 and in particular between 4:1 and 1:1. m e DA treatment is preferably carried out at a pressure in the range of between 20 and 100 bar. When n-butane is used as the sol-vent, the deasphalting is preferably carried out at a pressure of from 35-45 bar and a temperature of frcm 100-150C.
As noted hereinbefore, a subdivision of the embodiments belonging to class II, to which the present patent application 3o relates, may be made depending on whether stream 4 is used as feed or feed oomponent for the HT (class II~) or as feed or feed component for the DA treatment (class IIB). In the embodiments belonging to class IIA stream 2 is used as the feed for the 12069~
DA treatment. In the embodiments ~elonging to class IIB stream 3 is used as the feed for the ~T and stream 2 is used as a feed component for the TC treatment and/or as a feed component for the DA treatment.
m e various embod~ments belonging to class IIA are repre-sented schematically in Figure I. m e various streams, fractions and reaction zones are indicated by three digit numbers, the first of which refers to the Figure concerned. The vacuum residue (302~, for instance, refers to vacuum residue 2 in the context of Figure III. According to Figure I the process is carried out in an ap-paratus ccmprising a TC zone (lOS), a HT zone (106) and a DA zone (107), successively. An asphaltenes-containing hydrocarbon mixture (101) is subjected to a TC treatment and the cracked product is separated into one or more distillate fractions (108) and a resi-dual fraction (104). Stream 4 is subjected to a HT and the hydro-treated product is separated into one or more distillate fractions (109) and a residual fraction (102). Stream 2 is subjected to a DA
treatment and the product is separated into a deasphalted oil (110) and an asphaltic bitumen (103). In addition to this embodi-ment(IIA1), in which stream 103 is subjected to no further treat-ment, Figure I includes the follcwing three embodinents:
II~2 The use of at least part of stre~m 103 as a feed component for the TC treatment.
IIA3 The use of at least part of stream 103 as a feed component for the HT.
IIA4 The use of part of stream 103 as a feed component for the TC treatment and as a feed component for the HT.
12o69~6 m e various embodiments belonging to class IIB are repre-sented schematically in Figure II. According to this Figure the process is carried out in an apparatus comprising a TC zone (205), a DA zone (206) and a HT zone (207), successively. An asphaltenes-containing hydrocarbon mixture (201) is subjected to a TC treat-ment and the cracked product is separated into one or more dis-tillate fractions (208) and a residual fraction (204). Stream 204 is subjected to a DA treatment and the product is separated into a deasphalted oil (209) and an asphaltic bitumen (203). Stream 203 is subjected to a HT and the hydrotreated product is separated into one or more distillate fractions (210) and a residual frac-tion (202). Stream 202 is used either as a feed component for the TC treatment (embodiment IIBl) or as a feed CQmpOnent for the DA
treatment (embodiment IIB2) or as a feed component both for the TC
treatment and for the DA treatment (~nbodlTent IIB33.
In the embodiments aiming at the completest possible con-version of stream (.01) into deasphalted oil and hydrocarbon oil distillates, what is called a l'bleed stream" should preferably be separated f m m one of the heavy streams of the process. In that way the build-up during the process of undesirably heavy CQmpC-nents can be obviated.
Two flcw diagrams for the preparatio~ of deasphalted oil and hydrocar~on oil distillates from asphaltenes-containing hydro-carbon mixtures according to the invention will hereinafter be elucidated in more detail with the aid of Figures III and IV.
Flow diagLram A (based on embodiment IIB2) See Figure III.
The process is carried out in an apparatus comprising a TC zone composed of a thermal cracking unit ~305), an atmospheric dis-tillation unit (306) and a vacuum distillation unit (307), suc-cessively, a HT zone composed of a unit for catalytic hydro-treatment (308), a second atmospheric distillation unit (309) and a second vacuum distillation unit (310) and a DA zone t311). An asphaltenes-containing hydrocarbon mixture (301) is muxed with an asphaltic bitumen stream (312) and the mixture (313) is subjected to thermal cracking. m e cracked product (314) is separated by atmospheric distillation into a gas fraction (315), an atmospheric distillate (316) and an atmospheric residue (317). The atmospheric residue (317) is separated by vacuum distillation into a vacuum distillate (318) and a vacuum residue (304). The vacuum residue (304) is subjected together with hydrogen (319) to catalytic hydrotreatment. The hydrotreated product (320) is separated by atm~spheric distillation into a gas fraction (321), an atmospheric distillate (322) and an a~,~spheric residue (323). m e atm~spheric residue (323) is separated by vacuum distillation into a vacuum distillate (324) and a vacuum residue (302). The vacuum residue (302) is separated by solvent deasphalting into a deasphalted oil (325) and an asphaltic bitumen (303). The asphaltic bitumen (303) is divided into two portions (312) and (326).
Flow diaqram B (based on embodinent IIB1) See Figure IV.
The process is carried out in an apparatus compris m g a TC zone composed of a thermal cracking unit 1405), an atmospheric dis-tillation unit (406) and a vacuum distillation unit (407), suc-cessively, a DA zone (408) and a HT zone ccmposed of a unit for catalytic hydrotreatment (409), a second atmospheric dis-tillation unit (410) and a second vacuum distillation unit (411).
An asphaltenes-containing hydrocarbon muxture (401) is mixed with a vacuum residue (402) and the mixture 1412) is subjected to thermal cracking. The cracked product (413) is separated by atm~spheric distillation into a gas fraction (414), an atmospheric distillate (415) and an atmospheric residue (416). The atmospheric residue (416) is separated by vacuum distillation into a vacuum 12069t~6 distillate (417) and a vacuum residue (418). The vacuum residue (418) is separated by solvent deasphalting into a deasphalted oil (419) and an asphaltic bitumen (403). m e asphaltic bitumen (403) is divided into two portions (420) and (421). Portion (421) is subjected together with hydrogen (422) to catalytic hydrotreat-ment. m e hydrotreated product (423) is separated by atmospheric distillation into a gas fraction ~424), an atmospheric distillate (425) and an atmospheric residue (426~. m e atmospheric residue (426) is separated by vacuum distillation into a vacuum distillate (427) and a vacuum residue ~402).
The present patent application also includes apparatuses for carrying out the process according ~o the invention, which cor-respond substantially with those represented schematically by Figures I- IV.
The invention is now elucidated with the aid of the following Examples.
In the process according to the i~vention two asphaltenes-containing hydrocarbon mixtures obtained as residues in the vacuum distillation of atmospheric distillation residues frcm cxude mineral oils were used as the starting material. The vacuum residues both boiled substantially above 520C and they had RfT's of 18.2 and 12.3 %w. The process according to the invention was carried out according to flow diagrams A and B. The conditions used in the various zones were the follcwing.
In both the flcw diagrams the units for catalytic hydrotreat-ment consisted of two reactors, the first of which was filled with a Ni/V/SiO2 catalyst conta:ining 0.5 parts by weight (pbw) nickel and 2.0 pbw vanadium per 100 pbw silica and the second of which was filled with a Co/Mo/A1203 catalyst containing 4 pbw cobalt and 12 pbw moly~denum per 100 pbw alumina. The catalysts were used in a 1:4 volume ratio. The catalytic hydrotreatment was carried out at a hydrogen pressure of 150 bar, a space velocity (measured 3~2~906 over the two reactors) of 0.5 kg feed per litre catalyst per hour, a H2/feed ratio of 1000 Nl per kg and an average temperature of 410C in the first reactor and of 385C in the second reactor.
In both the flow diagrams the DA treatment was carried out using n-butane as the solvent, at a temperature of 115C, a pressure of 40 bar and a solvent/oil weight ratio of 3:1.
In both the flow diagrams the ~C treatment was carried out in a cracking coil at a pressure of 10 bar, a space velocity of 0.4 kg fresh feed per litre cracking coil volume per minute and a temperature of 485C (t~mperature measured at the outlet of the cracking coil).
Example 1 This Example was carried out according to flow diagr~m A as represented by Figure III.
100 pbw vacuum residue (301) having an R~T of 18.2 %w yielded the various streams in the following quantities:
115.8 pkw muxture (313), 15.0 " C5-350C atmospheric distillate (316), 98.6 " 350C~ atmospheric residue (317), 11.8 " 350-520C vacuum distillate (318), 86.8 " 520C+ vacuum residue (304) having an R~T of 34.6 ~w, a product (320), the C5 fraction of which had an RCT of 15.9 %w, 11.6 pbw C5-350C atmospheric distillate (322), 71.3 " 350C atmospheric residue (323), 17.4 " 350-520C vacuum distillate (324), 53.9 1l 520C~ vacuum residue (302), 29.1 " deasphalted oil (325), 24.8 " asphaltic bitumen (303), 15.8 " portion (312) and 9.0 " portion (326).
Example 2 This Example was carried out according to flow diagram B as represented by Figure IV.
100 pbw vacuum residue (401) having an RCT of 12.3 %w yielded ~2069~6 _he various streams in the following ~uantities:
113.1 pbw muxture (412), 18.8 " C5-350C atmDspheric distillate (415), 91.6 " 350C+ atm~spheric residue (416), 14.7 " 350-520C vacuum distillate (417~, 76.9 " 520C~ vacuwm residue (418), 46.1 " deasphalted oil (419~, 30.8 " asphaltic bitumen (403), 8.6 " portion (4203, 22.2 " portion (421) having an RCT of 50.0 ~w, a product (423), the C5 fraction of which had an RCT of 27.5 %w, 3.2 pbw C5-350C atm~spheric distillate (425), 17.9 " 350C+ atmospheric residue (426),
4.8 " 350-520C vacuum distillate (427), and 13.1 " 520C+ vacuum residue (402).
Claims (9)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the production of deasphalted oils and hydrocarbon oil distillates from asphaltenes-containing hydrocar-bon mixtures, characterized in that an asphaltenes-containing hydrocarbon mixture (stream 1) is subjected to a thermal cracking treatment (TC) in which a feed is converted into a product which contains less than 20%w C4- hydrocarbons and from which one or more distillate fraction and a heavy fraction (stream 4) are separated, that stream 4 is subjected to a combination of the following two treatments: a catalytic hydrotreatment (HT) in which an asphaltenes-containing feed is converted into a product which has a reduced asphaltenes content and from which one or more distillate fractions and a heavy fraction (stream 2) are separated and a solvent deasphalting treatment (DA) in which an asphaltenes-containing feed is converted into a product from which a deasphalted oil fraction and an asphaltic bitumen fraction (stream 3) are separated, and that stream 4 is used either 1) as feed or feed component for the HT, with stream 2 being used as the feed for the DA treatment, or 2) as feed or feed component for the DA treatment, with stream 3 being used as the feed for the HT and stream 2 as a feed com-ponent for the TC treatment and/or as a feed component for the DA treatment.
2. A process as claimed in claim 1, characterized in that stream 4 is used as feed or feed component for the HT and that at least part of stream 3 is used as a feed component for the TC
treatment and/or as a feed component for the HT.
treatment and/or as a feed component for the HT.
3. A process as claimed in claim 1, characterized in that a hydrocarbon mixture which boils substantially above 350°C and more than 35%w of which boils above 520°C and which has an RCT
of more than 7.5 %w, such as a residue obtained in the vacuum distillation of an atmospheric distillation residue from a crude mineral oil is used as stream 1.
of more than 7.5 %w, such as a residue obtained in the vacuum distillation of an atmospheric distillation residue from a crude mineral oil is used as stream 1.
4. A process as claimed in claim 1, characterized in that one or more vacuum distillates are separated from one or more of streams 1, 2 and 4.
5. A process as claimed in claim 1, characterized in that the catalyst used in the HT for the reduction of the asphaltenes content of the feed is a catalyst which comprises at least one metal chosen from the group formed by nickel and cobalt and in addition at least one metal chosen from the group formed by molybdenum and tungsten supported on a carrier, which carrier consists more than 40 %w of alumina.
6. A process as claimed in claim 1, characterized in that the HT is carried out at a temperature of from 350-450°C, a pressure of from 75-200 bar, a space velocity of from 0.1- 2 g.g-1.h-1 and a H2/feed ratio of from 500-2000 Nl.kg-1.
7. A process as claimed in claim 1, characterized in that the HT is carried out in such a way that it yields a product, the C5+ fraction of which meets the following requirements:
a) the RCT of the C5+ fraction amounts to 20-70% of the RCT of the feed and b) the difference between the percentages by weight of hydrocarbons boiling below 350°C present in the C5+ fraction and in the feed is at most 40.
a) the RCT of the C5+ fraction amounts to 20-70% of the RCT of the feed and b) the difference between the percentages by weight of hydrocarbons boiling below 350°C present in the C5+ fraction and in the feed is at most 40.
8. A process as claimed in claim 1, characterized in that the DA treatment is carried out using n-butane as the solvent at a pressure of from 35-45 bar and a temperature of 100-150°C.
9. A process as claimed in claim 1, characterized in that the TC treatment is carried out at a temperature of from 400-525°C
and a space velocity of from 0.01-5 kg fresh feed per litre cracking reactor volume per minute.
and a space velocity of from 0.01-5 kg fresh feed per litre cracking reactor volume per minute.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL8201243 | 1982-03-25 | ||
| NL8201243A NL8201243A (en) | 1982-03-25 | 1982-03-25 | PROCESS FOR THE PREPARATION OF LOW ASPHALTANE HYDROCARBON MIXTURE. |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1206906A true CA1206906A (en) | 1986-07-02 |
Family
ID=19839475
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000423215A Expired CA1206906A (en) | 1982-03-25 | 1983-03-09 | Process for the production of deasphalted oils and hydrocarbon distillates |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0090441B1 (en) |
| JP (1) | JPS58173191A (en) |
| AU (1) | AU552694B2 (en) |
| CA (1) | CA1206906A (en) |
| DE (1) | DE3360953D1 (en) |
| ES (1) | ES8401516A1 (en) |
| MX (1) | MX162479A (en) |
| NL (1) | NL8201243A (en) |
| ZA (1) | ZA831990B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1222471A (en) * | 1985-06-28 | 1987-06-02 | H. John Woods | Process for improving the yield of distillables in hydrogen donor diluent cracking |
| EP0779916B1 (en) * | 1994-09-05 | 1998-12-09 | Shell Internationale Researchmaatschappij B.V. | Process for the thermal cracking of a residual hydrocarbon oil |
| US6511937B1 (en) | 1999-10-12 | 2003-01-28 | Exxonmobil Research And Engineering Company | Combination slurry hydroconversion plus solvent deasphalting process for heavy oil upgrading wherein slurry catalyst is derived from solvent deasphalted rock |
| US6524469B1 (en) * | 2000-05-16 | 2003-02-25 | Trans Ionics Corporation | Heavy oil upgrading process |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL7512090A (en) * | 1975-10-15 | 1977-04-19 | Shell Int Research | PROCESS FOR CONVERTING HYDROCARBONS. |
| JPS559426U (en) * | 1978-07-04 | 1980-01-22 | ||
| NL190816C (en) * | 1978-07-07 | 1994-09-01 | Shell Int Research | Process for the preparation of gas oil. |
| JPS57123290A (en) * | 1981-01-25 | 1982-07-31 | Chiyoda Chem Eng & Constr Co Ltd | Method for converting heavy hydrocarbon oil into light fractions |
| NL8201119A (en) * | 1982-03-18 | 1983-10-17 | Shell Int Research | PROCESS FOR PREPARING HYDROCARBON OIL DISTILLATES |
-
1982
- 1982-03-25 NL NL8201243A patent/NL8201243A/en not_active Application Discontinuation
-
1983
- 1983-03-04 EP EP83200317A patent/EP0090441B1/en not_active Expired
- 1983-03-04 DE DE8383200317T patent/DE3360953D1/en not_active Expired
- 1983-03-09 CA CA000423215A patent/CA1206906A/en not_active Expired
- 1983-03-22 JP JP58046127A patent/JPS58173191A/en active Pending
- 1983-03-22 ES ES520830A patent/ES8401516A1/en not_active Expired
- 1983-03-22 AU AU12684/83A patent/AU552694B2/en not_active Ceased
- 1983-03-22 ZA ZA831990A patent/ZA831990B/en unknown
- 1983-03-24 MX MX196701A patent/MX162479A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| DE3360953D1 (en) | 1985-11-14 |
| JPS58173191A (en) | 1983-10-12 |
| EP0090441B1 (en) | 1985-10-09 |
| AU552694B2 (en) | 1986-06-12 |
| ES520830A0 (en) | 1983-12-16 |
| NL8201243A (en) | 1983-10-17 |
| AU1268483A (en) | 1983-09-29 |
| MX162479A (en) | 1991-05-13 |
| ES8401516A1 (en) | 1983-12-16 |
| ZA831990B (en) | 1983-11-30 |
| EP0090441A1 (en) | 1983-10-05 |
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