CA1176591A - Method of processing asphaltene-containing heavy hydrocarbon oils possibly having a high metal content - Google Patents
Method of processing asphaltene-containing heavy hydrocarbon oils possibly having a high metal contentInfo
- Publication number
- CA1176591A CA1176591A CA000378761A CA378761A CA1176591A CA 1176591 A CA1176591 A CA 1176591A CA 000378761 A CA000378761 A CA 000378761A CA 378761 A CA378761 A CA 378761A CA 1176591 A CA1176591 A CA 1176591A
- Authority
- CA
- Canada
- Prior art keywords
- oil
- feedstock
- residue
- donor solvent
- fraction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/22—Non-catalytic cracking in the presence of hydrogen
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
Landscapes
- 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)
Abstract
Metal 1003/JFW
ABSTRACT OF THE DISCLOSURE
A process for the processing of asphalt-containing heavy hydrocarbon oil feedstocks containing distillable fractions and residue is disclosed to obtain metal and asphaltene-free pro-ducts for use in the production of fuels and/or precursors for petrochemical products, while converting the residue nor-mally contained in such oil feedstocks to distillable products.
The oil feedstock which can be alternatively pretreated by vacuum distillation to obtain a residue together with a donor solvent is fed to a donor solvent hydrovishreaker followed by catalytic hydrotreatment of one or more distillate fractions obtained therefrom in a fixed bed reactor. In accordance with the invention, residue obtained from distillation of the donor solvent visbreaker effluent and donor solvent oil obtained from the hydrotreater are recycled to the donor solvent hydrovis-breaking, the naphthene content of the donor solvent oil being as high or higher than that of the distillable fractions of the feedstock, the proportion of donor solvent oil to the recycled hydrovisbreaker residue being selected so that the effective naphthene content of the combined feed is higher than that in the oil feedstock and the naphthene to residue concentration ratio in the mixed feed is the same or higher than its original value in the feedstock.
ABSTRACT OF THE DISCLOSURE
A process for the processing of asphalt-containing heavy hydrocarbon oil feedstocks containing distillable fractions and residue is disclosed to obtain metal and asphaltene-free pro-ducts for use in the production of fuels and/or precursors for petrochemical products, while converting the residue nor-mally contained in such oil feedstocks to distillable products.
The oil feedstock which can be alternatively pretreated by vacuum distillation to obtain a residue together with a donor solvent is fed to a donor solvent hydrovishreaker followed by catalytic hydrotreatment of one or more distillate fractions obtained therefrom in a fixed bed reactor. In accordance with the invention, residue obtained from distillation of the donor solvent visbreaker effluent and donor solvent oil obtained from the hydrotreater are recycled to the donor solvent hydrovis-breaking, the naphthene content of the donor solvent oil being as high or higher than that of the distillable fractions of the feedstock, the proportion of donor solvent oil to the recycled hydrovisbreaker residue being selected so that the effective naphthene content of the combined feed is higher than that in the oil feedstock and the naphthene to residue concentration ratio in the mixed feed is the same or higher than its original value in the feedstock.
Description
This invention relates to a method of processing asphaltene-containing heavy hydrocarbon oil feedstocks possibly having a metal content, such as crude oil, shale oil, tars resulting from the conversion of coal or recovered from tar sand, and bitumes, to obtain metal- and asphaltene-free products for use in the production of fuels and/or to obtain precursors for the production of petrochemical products by donor solvent hydrovisbreaking (DSV), followed by a catalytic hydrotreating of one or more distillate fractions.
~ 1 -- r '~ 3 :~ l ~ ~ -. ~ D~
. .
1 Discussion of Prior Art ,
~ 1 -- r '~ 3 :~ l ~ ~ -. ~ D~
. .
1 Discussion of Prior Art ,
2 The known methods of processing heavy hydrocarbon oils , ,
3 which have very high content,e.g., 50 % by weight and above, of , 4 hlgh boiling components ~componcnts boiling above 500C), 5 asphaltenes, heavy metals and/or arsenic group elements are ,.
6 unsatisfactory and not sufficiently versatile as regard the 7 distribution of yields and the removal of metal.
9 ¦ In accordance with known proposals, such raw materials :
lO ¦ are processed by an expensive catalytic hydrogenation,in the 11 ¦ liquid phase and/or by deasphalting in order to convert asphal-12 ¦ tenes and to remove catalyst poisons and to provide products 13 ¦ which can be processed further in existing plants in accordance i 14 ¦ with the state of the art. Those proposals involve the dis- ' 15 ¦ advantage that the catalytic hydrogenation in the liquid phase '~ , 16 ¦ gives rise to a problem regarding the regeneration of the 17 ¦ catalyst. That problem can be solved only with great difficulty , 18 ¦ as the feedstock has very high con-tents of asphaltenes, metals, 19 ¦ and trace elements. The use of discardable catalysts involves 20 ¦ a loss of catalyst and low hydrocarbon yields. Additiollally, 21 ¦ the activity of the discardable catalysts in question is often , , 22 inadequate and this can be compensated only by the use of high 23 reaction pressures and reaction temperatures so that the yield 24 and quality are reduced.
26 It is also known to deasphalt heavy hydrocarbon oil in 27 order to obtain hydrocarbon oils which are substantially free 28 `~ ' , ' 2 ;
__ .
~.~ 7~
from asphaltenes and can be p.rocessed further. That process has the disadvantage that the yields are greatly restricted and an excessively large asphalt fraction is obtained which can hardly be utilized. On the other hand, these proposals do not ensure the required removal of metal and trace elements from feedstocks having very high contents of asphaltenes, metals and/or other trace elements which constitute catalyst poisons (German Offenlegungsschrift 25 04 487, 25 04 488, U.S.
Patent 4.159.241, 2.726.490 ;German applications 2.664.721, 2.726.490).
It would be advantageous to have a method which permits the compliance with the desired quality requirements in conjunction with a high yield.
SUMMARY OF INVENTION
The present invention relates to a method incorporat-ing the use of donor solvent hydrovisbreaking (DSV), followed by catalytic hydrotreating, wherein the vacuum distillation residue in the oil feedstock is converted to distillate pro-ducts and wherein residue obtained by the distillation of the effluent from the donor solvent visbreaker and of donor solvent oil from the hydrotreater are recycled, said recycled streams and said oil feedstock being combined to a mixed feed and sub-jected to said hydrovisbreaking, the naphthene content of the donor solvent oil being as high as or higher than that of the distillable fractions of the oil feedstock, the proportion of the donor solvent oil to the recycled hydrovisbreaker residue being selected so that the effective naphthene content in the mixed feed is higher than that in the oil feedstock, and the naphthene-to-residue concentration weight ratio in the mixed feed being increased at least to its original value.
Within the scope of the invention, hydrovisbreaker distillate can be recycled rather than donor solvent oil from the hydrotreater.
~ lso within the scope of the invention, the vacuum distillation residue of the oil feedstock rather that the oil feedstock itself may be fed to the donor solvent hydrovisbreaker.
According to a preferred fur~her feature of the invention, the visbreaker distillate and a straight-run distil-late from the distillation of the oil feedstock are jointly catalytically hydrogenated in the hydrotreater.
According to a further preferred feature of the invention, the effluent from the donor solvent hydrovisbreaker is separated into liquid and vapor phases at the reaction pressure and reaction temperature of the hydrovisbreaker, the liquid phase is fed into a flashing zone to produce a flash distillate and a flash residue, and the flash distillate and the vapor phase obtained in the hot separator are jointly fed to the hydrotreater.
The donor solvent hydrovisbreaking and the hydro-treating are desirably carried out in a common gas cycle without a pressure drop.
According to a further preferred feature of the invention, part of the hydrogen-rich recycle gas for the donor solvent visbreaking together with make-up hydrogen is fed into the flashing zone.
In particular the present invention provides a process for converting an asphaltene-containing heavy hydro-carbon oil feedstock, at least 50% by weight of said feedstock boiling above 500C, said feedstock being crude oil, shale oil, tar resulting from the conversion of coal, tars recovered from tar sand, bitumen or a vacuum distillate residue thereof, which comprises the steps of:
A. mixing said feedstock with a donor solvent oil and a recycled residue to form a mixed feed, in said mixed feed the weight ratio of feed-stock to do~or solvent oil being 50:.38 to 20:~1 a~d the weight ratio of feedstock to recycled residue being 50-12 to 10.1, the naphthlenecontent of said mixed feed being higher than that in said feedstock;-B. feeding said mixed feed together with hydrogen into a donor solvent hydrovisbreaking zone opera-ting at a hydrogen pressure of between 50 and 250 bar and at temperatures between 400 and 450C and producing a hydrovisbreaker effluent;
C. subjecting said hydrovisbreaker effluent to a - first vacuum distillation and separately with-drawing a first gaseous fra.ction C5, a naphtha fraction, a distillate fraction boiling in the range of 200-250C and a residue fraction, mixing a partial stream of said residue fraction with said feedstock of step A as said recycled residue;
D. feeding said vacuum distillate fraction into a catalytic hydrotreating ~one operating at a hydro-yen pressure of between 70 and 200 bar and at temperatures in the range of 80 to 430C, and producing a hydrotreater effluent; and E. subjecting said hydrotreater effluent to a second vacuum distillation and separately withdrawing a second gaseous fraction C5, a fraction compose~
of naphtha, a fraction composed of diesel oil with a cetane number higher than 50, and a gas oil fraction with aConradson C value up to 0.1~ by weight and mixing at least a partial stream of said gas oil fraction with said feedstock of step A as said donor solvent oil.
1 ~ 7~
The advantages affordedby the process according to the invention over the knQwn proposals reside in that the problems involved in the regeneration o~ a catalyst for a hydrogenation in the liquid phase are eliminated, that the yield is not reduced by a loss of oil contained in discardable catalyst sludge, and that the conditions of donor solvent visbreaking no longer depend on the inactivation of the cata-lyst. Additionally, the invention permïts an optimum removal of metal and trace elements under mild conditions and in conjuction with a minimum consumption of hydrogen. The yields can be so adjusted that the quantity of visbreaker residue is in accordance with the requirements for the production of hydrogen.
Further advantages afford ~ ng - Sa -' ` ,2 11, ~'o~
1 to the invention over the known processes reside in that a 2 separation of the residue by distillation ensures a more reliable 3 demetallization in conjunction with unrestricted yields than a
6 unsatisfactory and not sufficiently versatile as regard the 7 distribution of yields and the removal of metal.
9 ¦ In accordance with known proposals, such raw materials :
lO ¦ are processed by an expensive catalytic hydrogenation,in the 11 ¦ liquid phase and/or by deasphalting in order to convert asphal-12 ¦ tenes and to remove catalyst poisons and to provide products 13 ¦ which can be processed further in existing plants in accordance i 14 ¦ with the state of the art. Those proposals involve the dis- ' 15 ¦ advantage that the catalytic hydrogenation in the liquid phase '~ , 16 ¦ gives rise to a problem regarding the regeneration of the 17 ¦ catalyst. That problem can be solved only with great difficulty , 18 ¦ as the feedstock has very high con-tents of asphaltenes, metals, 19 ¦ and trace elements. The use of discardable catalysts involves 20 ¦ a loss of catalyst and low hydrocarbon yields. Additiollally, 21 ¦ the activity of the discardable catalysts in question is often , , 22 inadequate and this can be compensated only by the use of high 23 reaction pressures and reaction temperatures so that the yield 24 and quality are reduced.
26 It is also known to deasphalt heavy hydrocarbon oil in 27 order to obtain hydrocarbon oils which are substantially free 28 `~ ' , ' 2 ;
__ .
~.~ 7~
from asphaltenes and can be p.rocessed further. That process has the disadvantage that the yields are greatly restricted and an excessively large asphalt fraction is obtained which can hardly be utilized. On the other hand, these proposals do not ensure the required removal of metal and trace elements from feedstocks having very high contents of asphaltenes, metals and/or other trace elements which constitute catalyst poisons (German Offenlegungsschrift 25 04 487, 25 04 488, U.S.
Patent 4.159.241, 2.726.490 ;German applications 2.664.721, 2.726.490).
It would be advantageous to have a method which permits the compliance with the desired quality requirements in conjunction with a high yield.
SUMMARY OF INVENTION
The present invention relates to a method incorporat-ing the use of donor solvent hydrovisbreaking (DSV), followed by catalytic hydrotreating, wherein the vacuum distillation residue in the oil feedstock is converted to distillate pro-ducts and wherein residue obtained by the distillation of the effluent from the donor solvent visbreaker and of donor solvent oil from the hydrotreater are recycled, said recycled streams and said oil feedstock being combined to a mixed feed and sub-jected to said hydrovisbreaking, the naphthene content of the donor solvent oil being as high as or higher than that of the distillable fractions of the oil feedstock, the proportion of the donor solvent oil to the recycled hydrovisbreaker residue being selected so that the effective naphthene content in the mixed feed is higher than that in the oil feedstock, and the naphthene-to-residue concentration weight ratio in the mixed feed being increased at least to its original value.
Within the scope of the invention, hydrovisbreaker distillate can be recycled rather than donor solvent oil from the hydrotreater.
~ lso within the scope of the invention, the vacuum distillation residue of the oil feedstock rather that the oil feedstock itself may be fed to the donor solvent hydrovisbreaker.
According to a preferred fur~her feature of the invention, the visbreaker distillate and a straight-run distil-late from the distillation of the oil feedstock are jointly catalytically hydrogenated in the hydrotreater.
According to a further preferred feature of the invention, the effluent from the donor solvent hydrovisbreaker is separated into liquid and vapor phases at the reaction pressure and reaction temperature of the hydrovisbreaker, the liquid phase is fed into a flashing zone to produce a flash distillate and a flash residue, and the flash distillate and the vapor phase obtained in the hot separator are jointly fed to the hydrotreater.
The donor solvent hydrovisbreaking and the hydro-treating are desirably carried out in a common gas cycle without a pressure drop.
According to a further preferred feature of the invention, part of the hydrogen-rich recycle gas for the donor solvent visbreaking together with make-up hydrogen is fed into the flashing zone.
In particular the present invention provides a process for converting an asphaltene-containing heavy hydro-carbon oil feedstock, at least 50% by weight of said feedstock boiling above 500C, said feedstock being crude oil, shale oil, tar resulting from the conversion of coal, tars recovered from tar sand, bitumen or a vacuum distillate residue thereof, which comprises the steps of:
A. mixing said feedstock with a donor solvent oil and a recycled residue to form a mixed feed, in said mixed feed the weight ratio of feed-stock to do~or solvent oil being 50:.38 to 20:~1 a~d the weight ratio of feedstock to recycled residue being 50-12 to 10.1, the naphthlenecontent of said mixed feed being higher than that in said feedstock;-B. feeding said mixed feed together with hydrogen into a donor solvent hydrovisbreaking zone opera-ting at a hydrogen pressure of between 50 and 250 bar and at temperatures between 400 and 450C and producing a hydrovisbreaker effluent;
C. subjecting said hydrovisbreaker effluent to a - first vacuum distillation and separately with-drawing a first gaseous fra.ction C5, a naphtha fraction, a distillate fraction boiling in the range of 200-250C and a residue fraction, mixing a partial stream of said residue fraction with said feedstock of step A as said recycled residue;
D. feeding said vacuum distillate fraction into a catalytic hydrotreating ~one operating at a hydro-yen pressure of between 70 and 200 bar and at temperatures in the range of 80 to 430C, and producing a hydrotreater effluent; and E. subjecting said hydrotreater effluent to a second vacuum distillation and separately withdrawing a second gaseous fraction C5, a fraction compose~
of naphtha, a fraction composed of diesel oil with a cetane number higher than 50, and a gas oil fraction with aConradson C value up to 0.1~ by weight and mixing at least a partial stream of said gas oil fraction with said feedstock of step A as said donor solvent oil.
1 ~ 7~
The advantages affordedby the process according to the invention over the knQwn proposals reside in that the problems involved in the regeneration o~ a catalyst for a hydrogenation in the liquid phase are eliminated, that the yield is not reduced by a loss of oil contained in discardable catalyst sludge, and that the conditions of donor solvent visbreaking no longer depend on the inactivation of the cata-lyst. Additionally, the invention permïts an optimum removal of metal and trace elements under mild conditions and in conjuction with a minimum consumption of hydrogen. The yields can be so adjusted that the quantity of visbreaker residue is in accordance with the requirements for the production of hydrogen.
Further advantages afford ~ ng - Sa -' ` ,2 11, ~'o~
1 to the invention over the known processes reside in that a 2 separation of the residue by distillation ensures a more reliable 3 demetallization in conjunction with unrestricted yields than a
4 deasphalting and that the processing is greatly simplified.
5 ~ ,
6 DESCRIP'rION ~F SPECIFIC EMBODIMENTS ;
7 ~
8 In carrying out the process the donor solvent hydro-
9 visbreakter is fed with oil feedstock having between 50 and 100 weight percent of components boiling above 500 C, these' 11 components normally remaining unconverted into distillable 12 products. The remainder of the oil comprises distillable fractions 13 of up to 500 C. The donor solvent hydrovisbreaker lS normally 14 operated at a hydrogen pressure of between 50 and 250 bars and 15 at a temperature between 400 and 450 C, The residence time of '~
16 the feedstock through the donor solvent hydrovisbreaker is 17 between 30 and 120 minutes. ~lternatively, instead of using an 18 oil feedstock there can be employed -the vacuum residue obtained 19 by subjecting such oil feedstock to vacuum distillation so that :
a straight-run distLllate is removed with a final boiling point 21 between 480 and 550 C corresponding to atmospheric pressure.
23 The effluent from the hydrovisbreaker is fed to a Z4 distillation zone to separate a fraction up to C5 and to obtain 25 further cuts, such as naphtha cutl having a boiling range of i 26 C6 to 200 C + 40 C, at least one middle distillate cut boiling 2~ - 6 -. I ~ f ~
1 ¦ between 200 + ~0 C and 500 ~ 30 C. ~ residue boiling above 2 1 500 + 30 C is obtained which is recycled in accordance with the 3 linvention.
¦ -The hydrotreater is normally operated at a hydrogen 6 ¦pressure of between 70 and 200 atmospheres and is maintained at a 7 ¦temperature of between 80 and 430 C. ~ hydrotreating catalyst 8 ¦such as nickel/molybdenum sulfide, supported on alumina, is ¦included in the form of a fixed bed in the hydrotreater, The
16 the feedstock through the donor solvent hydrovisbreaker is 17 between 30 and 120 minutes. ~lternatively, instead of using an 18 oil feedstock there can be employed -the vacuum residue obtained 19 by subjecting such oil feedstock to vacuum distillation so that :
a straight-run distLllate is removed with a final boiling point 21 between 480 and 550 C corresponding to atmospheric pressure.
23 The effluent from the hydrovisbreaker is fed to a Z4 distillation zone to separate a fraction up to C5 and to obtain 25 further cuts, such as naphtha cutl having a boiling range of i 26 C6 to 200 C + 40 C, at least one middle distillate cut boiling 2~ - 6 -. I ~ f ~
1 ¦ between 200 + ~0 C and 500 ~ 30 C. ~ residue boiling above 2 1 500 + 30 C is obtained which is recycled in accordance with the 3 linvention.
¦ -The hydrotreater is normally operated at a hydrogen 6 ¦pressure of between 70 and 200 atmospheres and is maintained at a 7 ¦temperature of between 80 and 430 C. ~ hydrotreating catalyst 8 ¦such as nickel/molybdenum sulfide, supported on alumina, is ¦included in the form of a fixed bed in the hydrotreater, The
10 ¦liquid hourly space velocity of the distillate being passed throug~
11 ¦the hydrotreater is between 0.5 and 2 LHSV.
12 I
13 ¦ Effluent from the hydrotreater is thereafter subjected
14 ¦to distillation to distill as overhead a C5-fraction. A naphtha containing fraction can also be taken off as a side cut. A diesel 16 oil side cut of boiling point between 180 + 20 C and 320 + 30 C
17 ¦can also be obtained. A residue is ob-tained from such hydro-18 ~treater comprising donor solvent oil which is vacuum gas oil.
19 ¦Donor solvent oil ls a topped effluent of the hydrotreater boiling 20 ¦above 180 + 20 C.
22 ¦ In a preferred mode of the invention, the residue 23 ¦obtained from distillation of the donor solvent hydrovisbreaker 24 effluent and the donor solvent oil are combined with the feed-stock to form a mixed feed to the donor solvent hydrovisbreaker;
26 The donor solvent has a naphthene content which is as high or ~ ~ ~ ~ --. .
1 higher than that of the distillable fractions of the feedstock 2 in donor solvent hydrovisbreaker. Generally speaking, the naph-~3 thene content of the donor solvent oil is between 10 and 50 4 weight % and in any event, it is at least as hiyh as the naphthe~
content of the distillable fractions of the oil feedstock.
6 Generally speaking, the naphthene content of the recycled donor 7 solvent oil is 1 to 1.5 times the naph-thene content of the 8 distillable fractions of the oil feedstock.
9 . ,, , .
The proportion of donor solvent oil to recycled hydro-11 visbreaker residue is selected so that the effective naphthene 12 content in the mixed feed is higher than that in the oil feed-13 stoc};. Generally speaking, the weight ratio of donor solvent oil 14 recycled to hydrovisbreaker residue recycled is 0.5 to 1.5 : 1.
By observing such ratio the effectlve naphthene content in the ,:
16 mixed féed is higher than that in the oil fcedstock and generally :~
17 between 1 and 1.2 times that of the naphthene content of the oil donor 18 feedstock to the/solvent hydrovisbreaker. By the term "effective 19 naphthene content" is meant the concentration of naphthenic bonded carbon fraction (percent) to the residue concentration 21 (percent by weight). By ensuring that the naphthene content in 22 the donor solvent oil is higher than the naphthene conten-t in 23 the distillable fraction of the oil feedstock, the naphthene to 24 residue concentration weight ratio can be adjusted to above its original value.
26 .
27 Instead of recycling donor solvcnt oil from the hydro-28 visbreaker, hydrovisbreaker distillate boiling in the range of - 8 -.
.
:~
. ~17~ l 1 200 to 500 C can be empfloyed ln lieu thereoE. ~lternatively, .
2 distillate from the dist.illation oE the hydrovisbreaker effluent .
3 can be used together with donor solvent oil obtained as topped ~' .
4 bottom from the distillation of the effluent from the hydrotreater.
When such.hydrovisbreaker distillate is employed it should be 6 employed in such a quantity to provide the naphthene contents in 7 the feed to the donor solvent hydrovisbreaker in accordance with 8 the conditions above. Generally speaking, the naphthene content 9 of the recycle to the donor solvent hydrovisbreaker is 10 to 30 % .
by weight based upon the combined weight of the solvent recycled 11 and the oil feedstock to the visbreaker. .
13 . In accordance with one embodiment of the invention, .
14 visbreaker distillate and distillate obtained from vacuum .
distillation of the oil feedstock can be jointly catalytically .
16 hydrogenated in the hydrotreater. Generally speaking, the distil-17 late obtained from the visbreaker eEfluent which is so-treated .
lB in the hydrotreater has a boiling point of between 200 and 500 C. .
19 The distillate obtained from distilla-tion of the oil feedstock is a straight-run distillate and generally boils in the range up .
21 to 560 C.
23 When the process is conducted by separating the vis-24 .breaker effluent into a liquid and vapor phase, flashing off of th vapor is effected by either increasing the hydrogen partial pres-. .
26 sure by adding at least a part of the recycle gas stream and the 2r . _ 9 _ ~
.
~ ! L
'.` .
. ~.'7t~5~ .
1 make-up hydrogerl or simultaneously heatillg the liquid feed of the 2 flashing zone. The specification implies there is no change in 3 the pressure and the temL~erature. It also implies that the vapor 4 phase from the donor solvent visbreaking are mixed with the flash distillate. In fact, the flash distillate is mixed witll distillate 6 obtained from distilling the flash r~sidue.
8 BRIEE DESCRIPTION Ol;` TI~E DRAWINGS
9 . .
In order to more fully appreciate the invention, 11 reference is made to the accompanying drawings in which:
13 Fig. 1 is a flow diagram of one mode of carrying out 14 the invention;
Fig. 2 is a flow diagram of another mode of carrying ~ ~;
16 out the invention;
17 Fig. 3 is a flow diagram oE stlll ano~:her mode of 18 carrying out the invention.
19 . - . .' In the drawings, gas cycles as well as heat exchange, 21 pressure conveying and pressure relief systems have been omitted 22 for the sake of clarity. This does not exclude the use for other ~3 combinations of the elements of the process according to the 24 invention, which combinations may be apparent to persons skilled in the art.
~ . r : ~ ~ ~
~ s~ ~
.
1 Example 1 ~
-2 .
3 In accordance with Figure 1, a feedstock 1 consisting, 4 e.g., of heavy fuel oil, as well as recycled donor oil 2 and vis-breaker residue 3 are fed to the donor solvent hydrovisbreaker 6 (DSV) 4 together with hydrogen, which was circulated together `J
7 with make-up and purge gas (not shown). The rate of the visbreaker 8 residue is 10 % by weight and the rate of donor oil is 5 % by 9 ¦weight relative to the feedstock 1~ The effluent 5 from the hydro-visbreaker is separated by distillation into the fractions C5 11 ~conduit 6), naphtha C6-200 C (conduit 7), vacuum distillate 12 20U - 500 C (conduit 8) an~ vacuum distillation residue (conduit 9).
131 .' . .
14 ¦ The hydrovisbreaker is operated, e.g., under the fol- ~
17 ¦can also be obtained. A residue is ob-tained from such hydro-18 ~treater comprising donor solvent oil which is vacuum gas oil.
19 ¦Donor solvent oil ls a topped effluent of the hydrotreater boiling 20 ¦above 180 + 20 C.
22 ¦ In a preferred mode of the invention, the residue 23 ¦obtained from distillation of the donor solvent hydrovisbreaker 24 effluent and the donor solvent oil are combined with the feed-stock to form a mixed feed to the donor solvent hydrovisbreaker;
26 The donor solvent has a naphthene content which is as high or ~ ~ ~ ~ --. .
1 higher than that of the distillable fractions of the feedstock 2 in donor solvent hydrovisbreaker. Generally speaking, the naph-~3 thene content of the donor solvent oil is between 10 and 50 4 weight % and in any event, it is at least as hiyh as the naphthe~
content of the distillable fractions of the oil feedstock.
6 Generally speaking, the naphthene content of the recycled donor 7 solvent oil is 1 to 1.5 times the naph-thene content of the 8 distillable fractions of the oil feedstock.
9 . ,, , .
The proportion of donor solvent oil to recycled hydro-11 visbreaker residue is selected so that the effective naphthene 12 content in the mixed feed is higher than that in the oil feed-13 stoc};. Generally speaking, the weight ratio of donor solvent oil 14 recycled to hydrovisbreaker residue recycled is 0.5 to 1.5 : 1.
By observing such ratio the effectlve naphthene content in the ,:
16 mixed féed is higher than that in the oil fcedstock and generally :~
17 between 1 and 1.2 times that of the naphthene content of the oil donor 18 feedstock to the/solvent hydrovisbreaker. By the term "effective 19 naphthene content" is meant the concentration of naphthenic bonded carbon fraction (percent) to the residue concentration 21 (percent by weight). By ensuring that the naphthene content in 22 the donor solvent oil is higher than the naphthene conten-t in 23 the distillable fraction of the oil feedstock, the naphthene to 24 residue concentration weight ratio can be adjusted to above its original value.
26 .
27 Instead of recycling donor solvcnt oil from the hydro-28 visbreaker, hydrovisbreaker distillate boiling in the range of - 8 -.
.
:~
. ~17~ l 1 200 to 500 C can be empfloyed ln lieu thereoE. ~lternatively, .
2 distillate from the dist.illation oE the hydrovisbreaker effluent .
3 can be used together with donor solvent oil obtained as topped ~' .
4 bottom from the distillation of the effluent from the hydrotreater.
When such.hydrovisbreaker distillate is employed it should be 6 employed in such a quantity to provide the naphthene contents in 7 the feed to the donor solvent hydrovisbreaker in accordance with 8 the conditions above. Generally speaking, the naphthene content 9 of the recycle to the donor solvent hydrovisbreaker is 10 to 30 % .
by weight based upon the combined weight of the solvent recycled 11 and the oil feedstock to the visbreaker. .
13 . In accordance with one embodiment of the invention, .
14 visbreaker distillate and distillate obtained from vacuum .
distillation of the oil feedstock can be jointly catalytically .
16 hydrogenated in the hydrotreater. Generally speaking, the distil-17 late obtained from the visbreaker eEfluent which is so-treated .
lB in the hydrotreater has a boiling point of between 200 and 500 C. .
19 The distillate obtained from distilla-tion of the oil feedstock is a straight-run distillate and generally boils in the range up .
21 to 560 C.
23 When the process is conducted by separating the vis-24 .breaker effluent into a liquid and vapor phase, flashing off of th vapor is effected by either increasing the hydrogen partial pres-. .
26 sure by adding at least a part of the recycle gas stream and the 2r . _ 9 _ ~
.
~ ! L
'.` .
. ~.'7t~5~ .
1 make-up hydrogerl or simultaneously heatillg the liquid feed of the 2 flashing zone. The specification implies there is no change in 3 the pressure and the temL~erature. It also implies that the vapor 4 phase from the donor solvent visbreaking are mixed with the flash distillate. In fact, the flash distillate is mixed witll distillate 6 obtained from distilling the flash r~sidue.
8 BRIEE DESCRIPTION Ol;` TI~E DRAWINGS
9 . .
In order to more fully appreciate the invention, 11 reference is made to the accompanying drawings in which:
13 Fig. 1 is a flow diagram of one mode of carrying out 14 the invention;
Fig. 2 is a flow diagram of another mode of carrying ~ ~;
16 out the invention;
17 Fig. 3 is a flow diagram oE stlll ano~:her mode of 18 carrying out the invention.
19 . - . .' In the drawings, gas cycles as well as heat exchange, 21 pressure conveying and pressure relief systems have been omitted 22 for the sake of clarity. This does not exclude the use for other ~3 combinations of the elements of the process according to the 24 invention, which combinations may be apparent to persons skilled in the art.
~ . r : ~ ~ ~
~ s~ ~
.
1 Example 1 ~
-2 .
3 In accordance with Figure 1, a feedstock 1 consisting, 4 e.g., of heavy fuel oil, as well as recycled donor oil 2 and vis-breaker residue 3 are fed to the donor solvent hydrovisbreaker 6 (DSV) 4 together with hydrogen, which was circulated together `J
7 with make-up and purge gas (not shown). The rate of the visbreaker 8 residue is 10 % by weight and the rate of donor oil is 5 % by 9 ¦weight relative to the feedstock 1~ The effluent 5 from the hydro-visbreaker is separated by distillation into the fractions C5 11 ~conduit 6), naphtha C6-200 C (conduit 7), vacuum distillate 12 20U - 500 C (conduit 8) an~ vacuum distillation residue (conduit 9).
131 .' . .
14 ¦ The hydrovisbreaker is operated, e.g., under the fol- ~
15 ¦lowing conditions: total pressure 140 bars; peak temperature :
16 1440 C; liquid space velocity in the soaker portion 0,8 kg/l.h; ;
17 ¦gas circulation rate l000 standard liters per kg of feedstock. , 1~ 1 : .
19 ¦ The vacuum distillate 8 is catalytically hydrogenated 20 ¦in the hydrotreater 10. The hydrotreater is operated, e.g., under 21 ¦the following conditions: Total pressure 175 bars; liquid hourly 22 ¦space velocity on catalyst bed 1 kg/l-h; peak temperature 415 C;
23 ¦gas circulation rate 700 standard liters per kg of feedstock.
24 ¦
25 ¦ The effluent from the hydrotreater 11 is separated by 26 ¦distillation into the fractions C5 (conduit 12), hydrotreater 27 l 2~ - 11 -. . . .' ;
~ 7 . . . .
1 naphtha (conduit 13), diesel oil (conduit 14) and vacuum gas oil 2 (conduit 15). The donor oil consists of the vacuum gas oil 3 fraction 15 and/or the diesel oil fraction 14. In the example, 4 the fractions contain more than 36 % by weight of naphthenes;
the straight-run distillate fraction of the oil feedstock con-6 tains less than 33 % by weight naphthenes, and the crude oil con-7 tains 35 ~ by weiqht of nap}lt}lelles.
9 In a naphtha-hydroyenating stage 16 the visbreaker naphtha 7 is processed in accordance with the state of the art to 11 obtain reformer feedstock or a motor gasoline component. The 12 hydrotreater naphtha 13 can be processed in the same step if all 13 naphtha that has been produced is to be reformed; otherwise the 14 naphtha can be directly used as a motor gasoline component. The diesel oil 14 has a cetane number higher than 50, a density up :
16 to 0.87 g/cm3 at 20 C and a sulfur content up to 0.05 % by , 17 weight. The vacuum gas oil 15 has a density of 0.91 g/cm3 at
19 ¦ The vacuum distillate 8 is catalytically hydrogenated 20 ¦in the hydrotreater 10. The hydrotreater is operated, e.g., under 21 ¦the following conditions: Total pressure 175 bars; liquid hourly 22 ¦space velocity on catalyst bed 1 kg/l-h; peak temperature 415 C;
23 ¦gas circulation rate 700 standard liters per kg of feedstock.
24 ¦
25 ¦ The effluent from the hydrotreater 11 is separated by 26 ¦distillation into the fractions C5 (conduit 12), hydrotreater 27 l 2~ - 11 -. . . .' ;
~ 7 . . . .
1 naphtha (conduit 13), diesel oil (conduit 14) and vacuum gas oil 2 (conduit 15). The donor oil consists of the vacuum gas oil 3 fraction 15 and/or the diesel oil fraction 14. In the example, 4 the fractions contain more than 36 % by weight of naphthenes;
the straight-run distillate fraction of the oil feedstock con-6 tains less than 33 % by weight naphthenes, and the crude oil con-7 tains 35 ~ by weiqht of nap}lt}lelles.
9 In a naphtha-hydroyenating stage 16 the visbreaker naphtha 7 is processed in accordance with the state of the art to 11 obtain reformer feedstock or a motor gasoline component. The 12 hydrotreater naphtha 13 can be processed in the same step if all 13 naphtha that has been produced is to be reformed; otherwise the 14 naphtha can be directly used as a motor gasoline component. The diesel oil 14 has a cetane number higher than 50, a density up :
16 to 0.87 g/cm3 at 20 C and a sulfur content up to 0.05 % by , 17 weight. The vacuum gas oil 15 has a density of 0.91 g/cm3 at
18 20 C, a sulfur content up to 0.05 ~ by weight,a Conradson C
19 value up to 0.1 % by weight and a metal content below 0.5 pp~ and :
is suitable as an FCC feedstock or as a raw material for lubri-21 cants (FCC = fluid catalytic converter).
23 The oil feedstock has a density of 1.01 g/cm3 at 20 C
24 and contains 65 % by weight of residue boiling above 500 C, 4 %
by weight sulfur and 500 ppm metal (V + Ni). The following frac-26 tions which were free from metal and asphaltenes were recovered 2~ - 12 -. . .
i~
1 from that oil feedstock: .
Z _ ', 3 C5 2 ~ by weight of feedstock 4 C6 up to ]70 C 20 % by weight oE feedstock 170 to 370 C 45 % by weight of feedstock 6 370 to 500 C 23 % by weight of feedstock. :
7 . .
8 The rate of visbreaker residue amounted to 10 % by 9 weight of the feedstock. .
11 Example 2 13 The method was carried out in -the saMe manner as in 14 Example 1 with the difference that the donor solvent hydrovis- .
breaker was fed with hydrovisbreakFr distillate 200 - 500 C at 16 a ~ate of 15 % by weight of the feedstock rather than with donor .
17 oil 2 composed of streams 14 and 15. That hydrovisbrealcer fraction .
18 17 contained 29 % by weight naphthenes. The yield of visbreaker 19 residue (VR~ in the overall method amounted to 25 % by weight of the feedstock.
22 Example 3 24 The method was carried out in accordance with Figure 2 and as.in Example 1 with the difference that the oil feedstock 1 .
26 was separated into a straight-run distillate fraction 2 and the 28 - 13 - .
~ . .
; ~ ~ ) :~
.~, ~ k ~
1 vacuum distillation residue 3. The latter was fed to the donor .
2 solvent hydrovisbreaker 4 together with hydrogen and with donor .
3 solvent oil from the hydrotreater effluent and the visbreaker .
4 residue 6. The visbreaker distillate 200 - 500 C (7) together 5 with the straight-run distillate 2 was catalytically hydro- .
6 genated in the hydrotreater 8. .
8 The fcedstock for the DSV stage 4 was composed of:
9 Vacuum distil]ation residuo 500 C +
from raw feedstock 50 % by weight 11 visbreaker residue 500 C (6) 12 % by welght i2 Donor solvent oil (5) 38 % by wei.ght 14 In that case the yield of visbreaker residue (VR) in .
the entire method was 15 % by weight oE the raw feedstock (1). ~
16 . . 'l' 17 Example 4 . .
19 The method was carried out in accordance with Figure 3
is suitable as an FCC feedstock or as a raw material for lubri-21 cants (FCC = fluid catalytic converter).
23 The oil feedstock has a density of 1.01 g/cm3 at 20 C
24 and contains 65 % by weight of residue boiling above 500 C, 4 %
by weight sulfur and 500 ppm metal (V + Ni). The following frac-26 tions which were free from metal and asphaltenes were recovered 2~ - 12 -. . .
i~
1 from that oil feedstock: .
Z _ ', 3 C5 2 ~ by weight of feedstock 4 C6 up to ]70 C 20 % by weight oE feedstock 170 to 370 C 45 % by weight of feedstock 6 370 to 500 C 23 % by weight of feedstock. :
7 . .
8 The rate of visbreaker residue amounted to 10 % by 9 weight of the feedstock. .
11 Example 2 13 The method was carried out in -the saMe manner as in 14 Example 1 with the difference that the donor solvent hydrovis- .
breaker was fed with hydrovisbreakFr distillate 200 - 500 C at 16 a ~ate of 15 % by weight of the feedstock rather than with donor .
17 oil 2 composed of streams 14 and 15. That hydrovisbrealcer fraction .
18 17 contained 29 % by weight naphthenes. The yield of visbreaker 19 residue (VR~ in the overall method amounted to 25 % by weight of the feedstock.
22 Example 3 24 The method was carried out in accordance with Figure 2 and as.in Example 1 with the difference that the oil feedstock 1 .
26 was separated into a straight-run distillate fraction 2 and the 28 - 13 - .
~ . .
; ~ ~ ) :~
.~, ~ k ~
1 vacuum distillation residue 3. The latter was fed to the donor .
2 solvent hydrovisbreaker 4 together with hydrogen and with donor .
3 solvent oil from the hydrotreater effluent and the visbreaker .
4 residue 6. The visbreaker distillate 200 - 500 C (7) together 5 with the straight-run distillate 2 was catalytically hydro- .
6 genated in the hydrotreater 8. .
8 The fcedstock for the DSV stage 4 was composed of:
9 Vacuum distil]ation residuo 500 C +
from raw feedstock 50 % by weight 11 visbreaker residue 500 C (6) 12 % by welght i2 Donor solvent oil (5) 38 % by wei.ght 14 In that case the yield of visbreaker residue (VR) in .
the entire method was 15 % by weight oE the raw feedstock (1). ~
16 . . 'l' 17 Example 4 . .
19 The method was carried out in accordance with Figure 3
20 and as in Example 1 with the difference that the effluent (1) .
21 from the donor solvent hydrovisbreaker (DSV) was separated in a
22 hot separator 2 into a vapor stream 3 and a liquid stream 4. The
23 latter was further separated in a flash distillation column 5
24 into a flash distillation residue 6 and a flashed-off distillate 7
25 witllout a pressure drop. The combined streams 3 and 7 were .
26 catalytically hydrogenated in the hydrotreater (HT) 8. In that .
27
28 - 14 -1 processing, the DSV and IIT stages were included in a gas cycle 9. .
2 A high-pressure separator 10 was usecl. Streams 11 and 12 consisted 3 of purge gas and of mclke-up hydroc3en, resL~cctively. Part of the . .
4 recycle gas was used toyether with the make-up hydrogen to 5 assist f lashing in column 5. .
~ . :
7 The same raw fee(istock was used as in ~xample 1. The 8 following yields related to raw feedstock were obtained:
9.
Vacuum distillation residue 500 C+ .
11 (flash distillation residue) 15 % by weight 12 Distillates:
13 Naphtha (n) + diesel oil (DO) + .
14 Vacuum gas oil (VGO) 76 % by weight .
1~ ! ~ 9 ~ by weight 22 . . .
. .
26 . .
1 . .
2 A high-pressure separator 10 was usecl. Streams 11 and 12 consisted 3 of purge gas and of mclke-up hydroc3en, resL~cctively. Part of the . .
4 recycle gas was used toyether with the make-up hydrogen to 5 assist f lashing in column 5. .
~ . :
7 The same raw fee(istock was used as in ~xample 1. The 8 following yields related to raw feedstock were obtained:
9.
Vacuum distillation residue 500 C+ .
11 (flash distillation residue) 15 % by weight 12 Distillates:
13 Naphtha (n) + diesel oil (DO) + .
14 Vacuum gas oil (VGO) 76 % by weight .
1~ ! ~ 9 ~ by weight 22 . . .
. .
26 . .
1 . .
Claims (3)
1. A process for converting an asphaltene-containing heavy hydrocarbon oil feedstock, at least 50% by weight of said feedstock boiling above 500°C, said feedstock being crude oil, shale oil, tar resulting from the conversion of coal, tars recovered from tar sand, bitumen or a vacuum distillate residue thereof, which comprises the steps of:
A. mixing said feedstock with a donor solvent oil and a recycled residue to form a mixed feed, in said mixed feed the weight ratio of feedstock to donor solvent oil being 50:38 to 20:.1 and the weight ratio of feedstock to recycled residue being 50:12 to 10:1 the naphthene content of said mixed feed being higher than that in said feedstock;
B. feeding said mixed feed together with hydrogen into a donor solvent hydrovisbreaking zone operating at a hydrogen pressure of between 50 and 250 bar and at temperatures between 400 and 450°C and producing a hydrovisbreaker effluent;
C. subjecting said hydrovisbreaker effluent to a first vacuum distillation and separately withdrawing a first gaseous fraction C5, a naphtha fraction, a distillate fraction boiling in the range of 200-500°C and a residue fraction, mixing a partial stream of said residue fraction with said feedstock of step A as said recycled residue;
D. feeding said vacuum distillate fraction into a cata-lytic hydrotreating zone operating at a hydrogen pressure of between 70 and 200 bar and at temperatures in the range of 80 to 430°C, and producing a hydro-treater effluent; and E. subjecting said hydrotreater effluent to a second vacuum distillation and separately withdrawing a second gaseous fraction C5, a fraction composed of naphtha, a fraction composed of diesel oil with a cetane number higher than 50, and a gas oil fraction with a Conradson C value up to 0.1% by weight and mixing at least a partial stream of said gas oil fraction with said feedstock of step A as said donor solvent oil.
A. mixing said feedstock with a donor solvent oil and a recycled residue to form a mixed feed, in said mixed feed the weight ratio of feedstock to donor solvent oil being 50:38 to 20:.1 and the weight ratio of feedstock to recycled residue being 50:12 to 10:1 the naphthene content of said mixed feed being higher than that in said feedstock;
B. feeding said mixed feed together with hydrogen into a donor solvent hydrovisbreaking zone operating at a hydrogen pressure of between 50 and 250 bar and at temperatures between 400 and 450°C and producing a hydrovisbreaker effluent;
C. subjecting said hydrovisbreaker effluent to a first vacuum distillation and separately withdrawing a first gaseous fraction C5, a naphtha fraction, a distillate fraction boiling in the range of 200-500°C and a residue fraction, mixing a partial stream of said residue fraction with said feedstock of step A as said recycled residue;
D. feeding said vacuum distillate fraction into a cata-lytic hydrotreating zone operating at a hydrogen pressure of between 70 and 200 bar and at temperatures in the range of 80 to 430°C, and producing a hydro-treater effluent; and E. subjecting said hydrotreater effluent to a second vacuum distillation and separately withdrawing a second gaseous fraction C5, a fraction composed of naphtha, a fraction composed of diesel oil with a cetane number higher than 50, and a gas oil fraction with a Conradson C value up to 0.1% by weight and mixing at least a partial stream of said gas oil fraction with said feedstock of step A as said donor solvent oil.
2. A process according to claim 1, wherein the oil feed-stock is initially subjected to a vacuum distillation and the vacuum distillation residue obtained therefrom is mixed with said donor solvent oil to form said mixed field of step A.
3. A process according to claim 2, wherein the effluent from said donor solvent hydrovisbreaking is subjected to vacuum distillation to obtain therefrom a number of distillate frac-tions and the straight-run distillate of the feedstock toge-ther with the distillate from said vacuum distillation of said effluent are jointly catalytically hydrogenated in said hydrotreater.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19803020518 DE3020518C2 (en) | 1980-05-30 | 1980-05-30 | Process for the processing of heavy, asphaltene-containing hydrocarbon oils |
| DEP3020518.6 | 1980-05-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1176591A true CA1176591A (en) | 1984-10-23 |
Family
ID=6103556
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000378761A Expired CA1176591A (en) | 1980-05-30 | 1981-06-01 | Method of processing asphaltene-containing heavy hydrocarbon oils possibly having a high metal content |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPS5716091A (en) |
| AU (1) | AU536302B2 (en) |
| CA (1) | CA1176591A (en) |
| DE (1) | DE3020518C2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2538814B1 (en) * | 1982-12-30 | 1986-06-27 | Inst Francais Du Petrole | PROCESS FOR TREATING HEAVY OIL OR HEAVY OIL FRACTION TO CONVERT THERE INTO LIGHTER FRACTIONS |
| FR2538811A1 (en) * | 1982-12-30 | 1984-07-06 | Inst Francais Du Petrole | PROCESS FOR TREATING HEAVY OIL OR HEAVY OIL FRACTION TO CONVERT THEM TO LOWER FRACTIONS |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2772221A (en) * | 1953-07-01 | 1956-11-27 | Exxon Research Engineering Co | Reacting heavy residual fuel with hydrogen donor diluents |
| US3252888A (en) * | 1962-11-06 | 1966-05-24 | Exxon Research Engineering Co | Conversion of hydrocarbons with the use of hydrogen donor diluents |
-
1980
- 1980-05-30 DE DE19803020518 patent/DE3020518C2/en not_active Expired
-
1981
- 1981-05-18 JP JP7478481A patent/JPS5716091A/en active Pending
- 1981-05-29 AU AU71162/81A patent/AU536302B2/en not_active Ceased
- 1981-06-01 CA CA000378761A patent/CA1176591A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE3020518C2 (en) | 1987-01-08 |
| AU7116281A (en) | 1981-12-03 |
| DE3020518A1 (en) | 1981-12-10 |
| AU536302B2 (en) | 1984-05-03 |
| JPS5716091A (en) | 1982-01-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10815437B2 (en) | Conversion of heavy fuel oil to chemicals | |
| AU2006299204B2 (en) | Hydrotreating and hydrocracking process and apparatus | |
| US4686028A (en) | Upgrading of high boiling hydrocarbons | |
| EP1785468B1 (en) | Resid hydrocracking methods | |
| US4065379A (en) | Process for the production of normally gaseous olefins | |
| US5059303A (en) | Oil stabilization | |
| CA2107375C (en) | Process for producing low viscosity lubricating base oil having high viscosity index | |
| US8333884B2 (en) | Partial conversion hydrocracking process and apparatus | |
| US4363716A (en) | Cracking of heavy carbonaceous liquid feedstocks utilizing hydrogen donor solvent | |
| US3671419A (en) | Upgrading of crude oil by combination processing | |
| US4257871A (en) | Use of vacuum residue in thermal cracking | |
| CA1195638A (en) | Process for the production of hydrocarbon oil distillates | |
| US4992163A (en) | Cat cracking feed preparation | |
| US4500416A (en) | Process for the preparation of hydrocarbon oil distillates | |
| EP0683218B1 (en) | Process for the conversion of a residual hydrocarbon oil | |
| US4395324A (en) | Thermal cracking with hydrogen donor diluent | |
| EP0697455B1 (en) | Process for producing a hydrowax | |
| CA1176591A (en) | Method of processing asphaltene-containing heavy hydrocarbon oils possibly having a high metal content | |
| CA2154313C (en) | Process for producing a hydrowax | |
| US4721557A (en) | Combination process for the conversion of a residual asphaltene-containing hydrocarbonaceous stream to maximize middle distillate production | |
| US4435274A (en) | Process for manufacturing gasoline with upgrading of hydrocarbon oils | |
| CA2149595C (en) | Process for the conversion of a residual hydrocarbon oil | |
| US4715947A (en) | Combination process for the conversion of a residual asphaltene-containing hydrocarbonaceous stream to maximize middle distillate production | |
| US4814064A (en) | Combination process for the conversion of a residual hydrocarbonaceous charge stock to produce middle distillate product | |
| US2854398A (en) | Preparation of catalytic cracking feed stocks |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |