CA1137909A - Process for the preparation of a feed for a catalytic cracking process - Google Patents
Process for the preparation of a feed for a catalytic cracking processInfo
- Publication number
- CA1137909A CA1137909A CA000323888A CA323888A CA1137909A CA 1137909 A CA1137909 A CA 1137909A CA 000323888 A CA000323888 A CA 000323888A CA 323888 A CA323888 A CA 323888A CA 1137909 A CA1137909 A CA 1137909A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- activity
- rct
- process according
- pbw
- Prior art date
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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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A B S T R A C T
Process for preparation of oil with a Ramsbottom Carbon Test value (RCT) lower than 5%, a nickel content lower than 1.0 ppmw and a vanadium content lower than 2.5 ppmw which is suitable as feed for a catalytic cracking process, Oil with a pentane asphaltenes content lower than 0.2% is hydrotreated.
If the RCT is higher than 5%, a catalyst with high activi-ty is used; if the RCT is lower than 5%, a catalyst with low activity is used.
Process for preparation of oil with a Ramsbottom Carbon Test value (RCT) lower than 5%, a nickel content lower than 1.0 ppmw and a vanadium content lower than 2.5 ppmw which is suitable as feed for a catalytic cracking process, Oil with a pentane asphaltenes content lower than 0.2% is hydrotreated.
If the RCT is higher than 5%, a catalyst with high activi-ty is used; if the RCT is lower than 5%, a catalyst with low activity is used.
Description
~3~37~
A PROCESS FOR THE PREPARATION OF A FEED FOR A
CATALYTIC CRAC~ING PROCESS
The invention relates to a process for the preparation of an oil with a Ramsbottom Carbon Test value (RCT) lower than 5~, a nickel oontent lower than 1.0 ppmw and a vanadium content lower than 2.5 ppmw, which s suitable for use as the feed for a catalytic cracking process, by catalytic hydrotreating of an oil whose RCT and/or nickel content and/or vanadium content are higher than the above-mentioned limits.
In the catalytio cracking of hydrocarbon m.xtures the composition of these mixtures must satisfy certain requirements to make the catalytic cracking process an economic proposition. If the metal content, in particu-lar that of nickel and vanadium, is higher than a cer-tain value (for nickel 1.0 pbw per million (ppmw) and ` 15 for vanadium 2.5 ppmw), lighter cracking products,such as methane, are formed in undesired quantities at the C09t of the yield of dssired gasoline components.
If the content of heavy rasidual components (for which the Ramsbottom Carbon Test value (RCT) is a yardstick) is too high, deposition of carbon on the cracking catalyst becomes excessive; the RCT generally needs to be below 5~.
For the preparation of a feed for catal~tic crack-~ng the starting material usually is a heavy hydrocarbon oil, such as a residual deasphalted mineral oil, and/or ~ ~ 3t~
a high-boiling oil obtained from a minera7 oil by flash distillation in vacuo (the so-called flashed distlllate).
When this deasphalted oil and~or ~lashed distillate did not satisfY the requirements of a feed for catalytic cracking as regards RCT and/or metal content, they were subjected to a hydrotreatment, in order to reduce RCT
and metal content. In this process hydrogen pressures of 100 and more bar were used, in order to ensure stable operation during the hydrotreatment. The necessity of working at these high hydrogen pressures is found to be a disadvantage, because expensiYe high-pressure units have to be used then, and the hydrogen consump-tion is high.
The invention provides a process in which, by using certain starting materials and catalysts, the hydrotreat-ment for the preparation of a ~eed sui~able for a cata-lytic craoking process can be carried out at a lower hydrogen pressure and with lo er hydrogen consumption.
The invention therefore provides a process for the preparation of an oil with a Ramsbottom Carbon Test value (RCT) lower than 5%, a nickel content lower than 1.0 ppmw and a vanadium content lower than ~.5 ppmw which is suit-able for use as the feed for a catalytic cracking process, comprising a catalytic hydrotreatment of an oi1 whose RCT and~or nickel content and/or vanadium content lie above the above-mentioned limits, which process is characterized in that a hydrocarbon oil which has a pentane asphaltenes content lower than 0.2~ ls hydrotreated, in that, if this hydrocarbon oil has an RCT higher than 5~, a catallst is used which has an activity in the benzene test to be described 'nereinafter of at least 0.15 ml.ml .h , and, if this hydrocarbon oil has an RCT lower than 5~, a catalyst is used whlch has an activity in the benzene test 7Ower than 0.15 ml.ml .h , and in that the hydrotreatment is carried out at a temperature of 300_450C and a hydro-~ 3~ 3 gen partial pressure of 10-70 bar.
The above-mentioned henzene test in which the catalyst activity is determined is a hydrogenation test that is carried out in a micro reactor with a quan~ity of catalyst between 0.5 and 2.0 g, the weight of which is ~nown precisely and which corresponds to 1.00 ml compacted catalyst. Benzene vapour and hydrogen that contain a small amount of H2S are conducted across the catalyst under the following conditions:
T= 400C; p=46 bar; H2/C6H6 molar ratio=20 The reaction produce is analysed by GLC. The catalyst activity is expressed as the first-order reaction velocity constant for benzene hydrogenation in ml benzene. (ml cat.) l.h 1 (or ml.ml l.h 1).
The pentane asphaltenes content is determined according to IP 143/57, which has been modified such that pentane is used instead of heptane.
If the hydrocarbon oil to be hydrogenated has an RCT higher than 5~, a catalyst has to be used with an activity in the benzene test of at least 0.15 ml.ml l.h 1. This activity is preferably in the range o 0.25-1.00 ml.ml l.h 1.
~0 Examples of catalysts having an activity in the benzene test of at least 0.15 ml.ml l.h 1 are combinations of nickel or cobalt with molybdenum or tungsten deposited on carriers. The metàls may be present as such, or in the form of compounds such as o~ides or sulphides. Aluminas r silicas or silica-aluminas may very conveniently be used as the carriers. Those catalysts are preferred which have nickel sulphide and molybdenum sulphide on alumina as the carrier, in particular catalysts that have 0.5-20 and preferably 2-10 pbw nickel and 3-60 and preferably 5-20 pbw ~.3~
molybdenum per 100 pbw alumina.
If the hydrocarbon oil to be hydrogenated has an - 3a -~ ~ .
~ 3~
RCT lower than 5~, but too high a nickel content and/or vanadium content to be suitable for use as the feed for a catalytic cracking process, a catalyst has to be used with an activity in the benzene test of less than 0.15 ml.ml .h , and this act vity is preferred to be 0.025-0.0005 ml.ml .h Examples of catalysts having an ac~ivity in the benzene test of less than 0.15 ml.ml .h are vanadium and combinations of nickel and vanadium, deposited on carriers. The metals may be present as such, or in the form of compounds such as oxides or sulphides. Aluminas, silicas or silica-aluminas may very conven-ently be used as the carriers. Those catalysts are preferred which have nickel sulphide and vanadium sulphide on silica as the carrier, in particular catalysts that have 0.1-10 pbw nickel and 1-20 pbw vanadium per 100 pbw silica.
Naturally, for the hydrogenat~on of hydrocarbon oils having an RCT lower than 5% the aforement'oned catalysts which are more act~ve in the benzene test (activity ~ 0.15 ml.ml .h ) may also be used. However this ii~ not attractive, beCause when using these catalysts which ha~e an activity in the benzene test that is higher than required, the hydrogen comsumption will be higher than when using the catalysts which are suitable according to the invention with an activity in the benzene test of less than 0.15 ml.ml .h The hydrotreatment is preferably carried out at a temperature of 350~400 C and a hydro~en partial 3 pressure of 30_60 bar. Space velocities of 0.1-5, in particular 0.3-2 kg feed per l catalyst per hour are Yery suitable.
When the aim ~s to prepare a feed for a catalytic cracking process from a short residue, i.e. a residue 3~ of a mineral oil distillation that has been obtained ~ 3~
a~ter the components boiling to about 520 C under atmospheric pressure have been removed in vacuo, this short residue must first be deasphalted to a pentane asphaltenes content lower than 0.2%. This can be achieved by deasphalting with propane, butane or pent-ane to the desired level, which can be controlled by means of the amount o~ deasphalting agent and/or the deasphalting temperature. The resultant hydrocarbon oil w~th a pentane asphaltenes content lower than 0.2 can then be catalytically hydrotreated according to the invention.
If it is intended to convert flashed distillates into a feed suitable for a catalytic cracking process, deasphalting may generally be omitted, because the pentane asphaltenes content is as a rule loNer than 0.2%. Which catalyst has to be used then depends on the RCT of the ~lashed distillate.
When a long residue ti.e. the residue o~ a mineral oil distillation that has been obtained a~ter the compo-nents boiling to about 350 C have been removed under atmospheric pressure~ is evaporated in vacuo, a flashed distillate is obtained. The remaining short residue can be deasphalted to a pentane asphaltenes content lower than 0.2~. If the deasphalted oil thus ~5 obtained has an RCT lower than 5%, it may be mixed with the flashed distillate (if the metal content of the latter is too high) and the mixture be subjected to a hydrotreatment with a catalyst which has an activity in the benzene test of less than 0.15 ml.ml .h I~ the RCT of the deasphalted oil just mentioned is higher than 5~, this oil may be hydrotreated separa-tely with a catalyst which has an activity in the benzene test of at least 0.15 ml.ml .h . However, this deasphalted oil also may be mixed with a component (particularly a ~lashed distillate) with a lower RCT.
" ; , ~ ; , : . , : . . . . ..
.
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If the mixture has an RCT lower than 5% but a nickel and/or vanadium content that is too high, it may be hydrotreated accordinæ to the invention with a catalyst having an activity in the benzene test of less than 0.15 ml.ml .h , which may lead to a considerable decrease in hydrogen consumption.
Naturally, it is also possible to mix an oil - whether or not deasphalted - which has a pentane asphaltenes content higher than 0.2% with an oil having a lower pentane asphaltenes content, for instance a flashed distillate, to form a mixture with a C5 asphal-tenes content lower than 0.2%, and to sub~ect this mixture to a hydrotreatment aocordinK to the invention.
The oil obtained according to the process of the invention with an RCT lower than 5%, a nlckel content 1ower than 0.5 ppmw and a vanadium content lower than
A PROCESS FOR THE PREPARATION OF A FEED FOR A
CATALYTIC CRAC~ING PROCESS
The invention relates to a process for the preparation of an oil with a Ramsbottom Carbon Test value (RCT) lower than 5~, a nickel oontent lower than 1.0 ppmw and a vanadium content lower than 2.5 ppmw, which s suitable for use as the feed for a catalytic cracking process, by catalytic hydrotreating of an oil whose RCT and/or nickel content and/or vanadium content are higher than the above-mentioned limits.
In the catalytio cracking of hydrocarbon m.xtures the composition of these mixtures must satisfy certain requirements to make the catalytic cracking process an economic proposition. If the metal content, in particu-lar that of nickel and vanadium, is higher than a cer-tain value (for nickel 1.0 pbw per million (ppmw) and ` 15 for vanadium 2.5 ppmw), lighter cracking products,such as methane, are formed in undesired quantities at the C09t of the yield of dssired gasoline components.
If the content of heavy rasidual components (for which the Ramsbottom Carbon Test value (RCT) is a yardstick) is too high, deposition of carbon on the cracking catalyst becomes excessive; the RCT generally needs to be below 5~.
For the preparation of a feed for catal~tic crack-~ng the starting material usually is a heavy hydrocarbon oil, such as a residual deasphalted mineral oil, and/or ~ ~ 3t~
a high-boiling oil obtained from a minera7 oil by flash distillation in vacuo (the so-called flashed distlllate).
When this deasphalted oil and~or ~lashed distillate did not satisfY the requirements of a feed for catalytic cracking as regards RCT and/or metal content, they were subjected to a hydrotreatment, in order to reduce RCT
and metal content. In this process hydrogen pressures of 100 and more bar were used, in order to ensure stable operation during the hydrotreatment. The necessity of working at these high hydrogen pressures is found to be a disadvantage, because expensiYe high-pressure units have to be used then, and the hydrogen consump-tion is high.
The invention provides a process in which, by using certain starting materials and catalysts, the hydrotreat-ment for the preparation of a ~eed sui~able for a cata-lytic craoking process can be carried out at a lower hydrogen pressure and with lo er hydrogen consumption.
The invention therefore provides a process for the preparation of an oil with a Ramsbottom Carbon Test value (RCT) lower than 5%, a nickel content lower than 1.0 ppmw and a vanadium content lower than ~.5 ppmw which is suit-able for use as the feed for a catalytic cracking process, comprising a catalytic hydrotreatment of an oi1 whose RCT and~or nickel content and/or vanadium content lie above the above-mentioned limits, which process is characterized in that a hydrocarbon oil which has a pentane asphaltenes content lower than 0.2~ ls hydrotreated, in that, if this hydrocarbon oil has an RCT higher than 5~, a catallst is used which has an activity in the benzene test to be described 'nereinafter of at least 0.15 ml.ml .h , and, if this hydrocarbon oil has an RCT lower than 5~, a catalyst is used whlch has an activity in the benzene test 7Ower than 0.15 ml.ml .h , and in that the hydrotreatment is carried out at a temperature of 300_450C and a hydro-~ 3~ 3 gen partial pressure of 10-70 bar.
The above-mentioned henzene test in which the catalyst activity is determined is a hydrogenation test that is carried out in a micro reactor with a quan~ity of catalyst between 0.5 and 2.0 g, the weight of which is ~nown precisely and which corresponds to 1.00 ml compacted catalyst. Benzene vapour and hydrogen that contain a small amount of H2S are conducted across the catalyst under the following conditions:
T= 400C; p=46 bar; H2/C6H6 molar ratio=20 The reaction produce is analysed by GLC. The catalyst activity is expressed as the first-order reaction velocity constant for benzene hydrogenation in ml benzene. (ml cat.) l.h 1 (or ml.ml l.h 1).
The pentane asphaltenes content is determined according to IP 143/57, which has been modified such that pentane is used instead of heptane.
If the hydrocarbon oil to be hydrogenated has an RCT higher than 5~, a catalyst has to be used with an activity in the benzene test of at least 0.15 ml.ml l.h 1. This activity is preferably in the range o 0.25-1.00 ml.ml l.h 1.
~0 Examples of catalysts having an activity in the benzene test of at least 0.15 ml.ml l.h 1 are combinations of nickel or cobalt with molybdenum or tungsten deposited on carriers. The metàls may be present as such, or in the form of compounds such as o~ides or sulphides. Aluminas r silicas or silica-aluminas may very conveniently be used as the carriers. Those catalysts are preferred which have nickel sulphide and molybdenum sulphide on alumina as the carrier, in particular catalysts that have 0.5-20 and preferably 2-10 pbw nickel and 3-60 and preferably 5-20 pbw ~.3~
molybdenum per 100 pbw alumina.
If the hydrocarbon oil to be hydrogenated has an - 3a -~ ~ .
~ 3~
RCT lower than 5~, but too high a nickel content and/or vanadium content to be suitable for use as the feed for a catalytic cracking process, a catalyst has to be used with an activity in the benzene test of less than 0.15 ml.ml .h , and this act vity is preferred to be 0.025-0.0005 ml.ml .h Examples of catalysts having an ac~ivity in the benzene test of less than 0.15 ml.ml .h are vanadium and combinations of nickel and vanadium, deposited on carriers. The metals may be present as such, or in the form of compounds such as oxides or sulphides. Aluminas, silicas or silica-aluminas may very conven-ently be used as the carriers. Those catalysts are preferred which have nickel sulphide and vanadium sulphide on silica as the carrier, in particular catalysts that have 0.1-10 pbw nickel and 1-20 pbw vanadium per 100 pbw silica.
Naturally, for the hydrogenat~on of hydrocarbon oils having an RCT lower than 5% the aforement'oned catalysts which are more act~ve in the benzene test (activity ~ 0.15 ml.ml .h ) may also be used. However this ii~ not attractive, beCause when using these catalysts which ha~e an activity in the benzene test that is higher than required, the hydrogen comsumption will be higher than when using the catalysts which are suitable according to the invention with an activity in the benzene test of less than 0.15 ml.ml .h The hydrotreatment is preferably carried out at a temperature of 350~400 C and a hydro~en partial 3 pressure of 30_60 bar. Space velocities of 0.1-5, in particular 0.3-2 kg feed per l catalyst per hour are Yery suitable.
When the aim ~s to prepare a feed for a catalytic cracking process from a short residue, i.e. a residue 3~ of a mineral oil distillation that has been obtained ~ 3~
a~ter the components boiling to about 520 C under atmospheric pressure have been removed in vacuo, this short residue must first be deasphalted to a pentane asphaltenes content lower than 0.2%. This can be achieved by deasphalting with propane, butane or pent-ane to the desired level, which can be controlled by means of the amount o~ deasphalting agent and/or the deasphalting temperature. The resultant hydrocarbon oil w~th a pentane asphaltenes content lower than 0.2 can then be catalytically hydrotreated according to the invention.
If it is intended to convert flashed distillates into a feed suitable for a catalytic cracking process, deasphalting may generally be omitted, because the pentane asphaltenes content is as a rule loNer than 0.2%. Which catalyst has to be used then depends on the RCT of the ~lashed distillate.
When a long residue ti.e. the residue o~ a mineral oil distillation that has been obtained a~ter the compo-nents boiling to about 350 C have been removed under atmospheric pressure~ is evaporated in vacuo, a flashed distillate is obtained. The remaining short residue can be deasphalted to a pentane asphaltenes content lower than 0.2~. If the deasphalted oil thus ~5 obtained has an RCT lower than 5%, it may be mixed with the flashed distillate (if the metal content of the latter is too high) and the mixture be subjected to a hydrotreatment with a catalyst which has an activity in the benzene test of less than 0.15 ml.ml .h I~ the RCT of the deasphalted oil just mentioned is higher than 5~, this oil may be hydrotreated separa-tely with a catalyst which has an activity in the benzene test of at least 0.15 ml.ml .h . However, this deasphalted oil also may be mixed with a component (particularly a ~lashed distillate) with a lower RCT.
" ; , ~ ; , : . , : . . . . ..
.
~3~
If the mixture has an RCT lower than 5% but a nickel and/or vanadium content that is too high, it may be hydrotreated accordinæ to the invention with a catalyst having an activity in the benzene test of less than 0.15 ml.ml .h , which may lead to a considerable decrease in hydrogen consumption.
Naturally, it is also possible to mix an oil - whether or not deasphalted - which has a pentane asphaltenes content higher than 0.2% with an oil having a lower pentane asphaltenes content, for instance a flashed distillate, to form a mixture with a C5 asphal-tenes content lower than 0.2%, and to sub~ect this mixture to a hydrotreatment aocordinK to the invention.
The oil obtained according to the process of the invention with an RCT lower than 5%, a nlckel content 1ower than 0.5 ppmw and a vanadium content lower than
2.5 ppmw can very conveniently be used as the feed in a catalytic cracking process with the aid of an acldic catalyst, such as a silica-alumina or a molecular sieve, ~ at temperatures in the range 450-550C.
Example:
A number of experiments were carried out with the aid of two catalysts, viz. a sulphided catalyst which contained 4.3 pbw nickel and 10.9 pbw molybdenum on ~5 100 pbw alumina and which had an activity in the benzene test of 0.61 (catalyst A), and a sulphided catalyst which ontained 0.5 pbw nickel and 2 pbw vanadium on 100 pbw silica and which had an activity in the benzene test o~ 0.020/catalyst B).
Example:
A number of experiments were carried out with the aid of two catalysts, viz. a sulphided catalyst which contained 4.3 pbw nickel and 10.9 pbw molybdenum on ~5 100 pbw alumina and which had an activity in the benzene test of 0.61 (catalyst A), and a sulphided catalyst which ontained 0.5 pbw nickel and 2 pbw vanadium on 100 pbw silica and which had an activity in the benzene test o~ 0.020/catalyst B).
3 The starting materials used were deasphalted oils (DAO'S) and a flashed distillate (FD); the asphaltenes contents, RCT and nickel and vanadium contents are listed in the table. The starting materials were sub--" jected to a hydrotreatment at temperatures and pres-sures given in the table. In all cases the space ::
~.3~3~
ve~ocity was 0.5 ~g feed per litre catalyst per hour.
Experiments 4, 7 and 9 in the table are experiments according to the invention; the other experiments have been included for comparison.
Experiments 1, 2 and 3 show that no product is obtained with an RCT lower than 5% at C5 asphaltenes contents of 0.5~ (i.e. higher than according to the invention) at hydrogen partial pressures lower than 90 bar, or, in other words, that hydrogenation at a pressure of 10-70 bar (as is possible according to the invention) does not lead to the desired result with starting oaterials with too high a pentane asphaltenes content.
Experiment 4 (accordin8 to the invention) proves that with 2 catalyst having an activity in the benzene test higher than 0.5 ml.ml .h a starting material with an RCT of 8~ can be successfully hydrotreated.
Experiment 5 shows that catalyst B with an activity in the benzene test lower than 0.15 ml.ml .h fails and that the RCT cannot be reduced below 5~ with this catalyst.
From Experiment 6 it appears that a ~tarting material with an RCT lower than 5~ can be hydrotreated with catalyst A, but that the hydrogen consumption is muoh higher than when such a starting material is ~5 treated with catalyst B according to the invention (experiment 7).
Experiment 8 and experiment 9 (according to the invention) show the same difference in the treatment of a flashed distillate;`here again it is preferred to use oatalyst ~, because of the much lower hydrogen consumption.
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ve~ocity was 0.5 ~g feed per litre catalyst per hour.
Experiments 4, 7 and 9 in the table are experiments according to the invention; the other experiments have been included for comparison.
Experiments 1, 2 and 3 show that no product is obtained with an RCT lower than 5% at C5 asphaltenes contents of 0.5~ (i.e. higher than according to the invention) at hydrogen partial pressures lower than 90 bar, or, in other words, that hydrogenation at a pressure of 10-70 bar (as is possible according to the invention) does not lead to the desired result with starting oaterials with too high a pentane asphaltenes content.
Experiment 4 (accordin8 to the invention) proves that with 2 catalyst having an activity in the benzene test higher than 0.5 ml.ml .h a starting material with an RCT of 8~ can be successfully hydrotreated.
Experiment 5 shows that catalyst B with an activity in the benzene test lower than 0.15 ml.ml .h fails and that the RCT cannot be reduced below 5~ with this catalyst.
From Experiment 6 it appears that a ~tarting material with an RCT lower than 5~ can be hydrotreated with catalyst A, but that the hydrogen consumption is muoh higher than when such a starting material is ~5 treated with catalyst B according to the invention (experiment 7).
Experiment 8 and experiment 9 (according to the invention) show the same difference in the treatment of a flashed distillate;`here again it is preferred to use oatalyst ~, because of the much lower hydrogen consumption.
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Claims (9)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the preparation of an oil with a Ramsbottom Carbon Test value (RCT) lower than 5%, a nickel content lower than 1.0 ppmw and a vanadium content lower than 2.5 ppmw which is suit-able for use as the feed for a catalytic cracking process, compris-ing a catalytic hydrotreatment of an oil whose RCT and/or nickel content and/or vanadium content lie above the above-mentioned limits, characterized in that a hydrocarbon oil which has a pentane asphaltenes content lower than 0.2% is hydrotreated, in that, if this hydrocarbon oil has an RCT higher than 5%, a catalyst is used which has an activity in the benzene test,expressed as the first order reaction velocity constant for benzene hydrogenation in m1 benzene.
(m1 cat-1) .h-1 (or m1.m1-l.h-1), of at least 0.15 m1.m1-l.h-1, and, if this hydrocarbon oil has an RCT lower than 5%, a catalyst is used which has an activity in the benzene test lower than 0.15 m1.m1-1.h-1, and in that the hydrotreatment is carried out at a temperature of 300-450°C and a hydrogen partial pressure of 10-70 bar.
(m1 cat-1) .h-1 (or m1.m1-l.h-1), of at least 0.15 m1.m1-l.h-1, and, if this hydrocarbon oil has an RCT lower than 5%, a catalyst is used which has an activity in the benzene test lower than 0.15 m1.m1-1.h-1, and in that the hydrotreatment is carried out at a temperature of 300-450°C and a hydrogen partial pressure of 10-70 bar.
2. A process according to claim 1, characterized in that the catalyst which has an activity in the benzene test of at least 0.15m1.m1-1.h-1 has an activity of 0.25-1.00 m1.m1-1.h-1.
3. A process according to claim 1 or 2, characterized in that use is made of a catalyst with an activity in the benzene test of at least 0.15 m1.m1-l.h-1 which has nickel sulphide and molybdenum sulphide on alumina as the carrier.
4. A process according to claim 3, characterized in that the catalyst contains 2-10 pbw nicel and 5-20 pbw molybdenum per 100 pbw alumina.
5. A process according to claim 1, characterized in that the catalyst with an activity in the benzene test of less than 0.15 ml.ml-l.h-1 has an activity of 0.025-0.0005 ml.ml-l.h-1.
6. A process according to claim 5, characterized in that the catalyst with an activity in the benzene test lower than 0.15 ml.ml-l.h-1 consists of a silica carrier on which nickel and vanadium are deposited.
7. A process according to claim 6, characterized in that the catalyst contains 0.1-10 pbw nickel and 1-20 pbw vanadium per 100 pbw silica.
8. A process according to claim 1, characterized in that the hydrotreatment is carried out at a temperature of 350-400°C.
9. A process according to claim 1, characterized in that the hydrotreatment is carried out at a hydrogen partial pressure of 30-60 bar.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7805421BA NL7805421A (en) | 1978-05-19 | 1978-05-19 | PROCESS FOR THE PREPARATION OF A FOOD FOR A CATALYTIC CRACKING PROCESS. |
| NL7805421 | 1978-05-19 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1137909A true CA1137909A (en) | 1982-12-21 |
Family
ID=19830868
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000323888A Expired CA1137909A (en) | 1978-05-19 | 1979-03-21 | Process for the preparation of a feed for a catalytic cracking process |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS54152003A (en) |
| CA (1) | CA1137909A (en) |
| DE (1) | DE2920007A1 (en) |
| FR (1) | FR2426078A1 (en) |
| GB (1) | GB2022132B (en) |
| IT (1) | IT1114248B (en) |
| NL (1) | NL7805421A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3279051D1 (en) * | 1981-06-25 | 1988-10-27 | Shell Int Research | Process for the preparation of a hydrocarbon mixture |
| DE102010063191A1 (en) | 2010-12-16 | 2012-06-21 | Bayerische Motoren Werke Aktiengesellschaft | Internal combustion engine i.e. single-cylinder four-stroke internal combustion engine, for driving motorcycle, has radially running channel directed in position of crankshaft, where axially running channel of engine is part of channels |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE508479A (en) * | ||||
| US2925374A (en) * | 1958-05-19 | 1960-02-16 | Exxon Research Engineering Co | Hydrocarbon treating process |
| US3227645A (en) * | 1962-01-22 | 1966-01-04 | Chevron Res | Combined process for metal removal and hydrocracking of high boiling oils |
| US3553106A (en) * | 1968-06-28 | 1971-01-05 | Gulf Research Development Co | Catalytic removal of vanadium and nickel from oils |
| NL7012520A (en) * | 1969-08-25 | 1971-03-01 | ||
| US3716479A (en) * | 1970-12-23 | 1973-02-13 | Mobil Oil Corp | Demetalation of hydrocarbon charge stocks |
| JPS4920201A (en) * | 1972-06-19 | 1974-02-22 | ||
| JPS525693A (en) * | 1975-07-02 | 1977-01-17 | Nippon Oil Co Ltd | Catalyst for purification of raw material containing hydrocarbons by h ydrogenation |
-
1978
- 1978-05-19 NL NL7805421BA patent/NL7805421A/en not_active Application Discontinuation
-
1979
- 1979-03-21 CA CA000323888A patent/CA1137909A/en not_active Expired
- 1979-05-17 GB GB7917241A patent/GB2022132B/en not_active Expired
- 1979-05-17 DE DE19792920007 patent/DE2920007A1/en active Granted
- 1979-05-17 IT IT22745/79A patent/IT1114248B/en active
- 1979-05-17 FR FR7912594A patent/FR2426078A1/en active Granted
- 1979-05-17 JP JP5980379A patent/JPS54152003A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| FR2426078B1 (en) | 1984-11-23 |
| GB2022132B (en) | 1982-08-18 |
| DE2920007A1 (en) | 1979-11-29 |
| FR2426078A1 (en) | 1979-12-14 |
| GB2022132A (en) | 1979-12-12 |
| JPS54152003A (en) | 1979-11-29 |
| NL7805421A (en) | 1979-11-21 |
| IT7922745A0 (en) | 1979-05-17 |
| JPH0237384B2 (en) | 1990-08-23 |
| DE2920007C2 (en) | 1987-10-22 |
| IT1114248B (en) | 1986-01-27 |
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Legal Events
| Date | Code | Title | Description |
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| MKEX | Expiry |