CA1207696A - Start-up method for a hydrorefining process - Google Patents
Start-up method for a hydrorefining processInfo
- Publication number
- CA1207696A CA1207696A CA000445234A CA445234A CA1207696A CA 1207696 A CA1207696 A CA 1207696A CA 000445234 A CA000445234 A CA 000445234A CA 445234 A CA445234 A CA 445234A CA 1207696 A CA1207696 A CA 1207696A
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- Prior art keywords
- catalyst
- oil
- heavy
- hydrorefining
- contacting
- Prior art date
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Abstract
ABSTRACT OF THE DISCLOSURE
A hydrorefining process for heavy hydrocar-bonaceous oils, such as gas oils, is initiated by contacting a sulfided hydrorefining catalyst, such as nickel-molybdenum on alumina, with a light hydrocarbon-aceous oil boiling in the range of C5 to 700°F, in the presence of hydrogen, at specified conditions and, thereafter, contacting the catalyst with the heavy hydrocarbonaceous oil to be hydrorefined.
A hydrorefining process for heavy hydrocar-bonaceous oils, such as gas oils, is initiated by contacting a sulfided hydrorefining catalyst, such as nickel-molybdenum on alumina, with a light hydrocarbon-aceous oil boiling in the range of C5 to 700°F, in the presence of hydrogen, at specified conditions and, thereafter, contacting the catalyst with the heavy hydrocarbonaceous oil to be hydrorefined.
Description
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BACKGROUND OF THE INVENTION
BACKGROUND OF THE INVENTION
2 1. Field of the Invention
3 This invention relates ~o a start-up process
4 for hydrorefining heavy hydrocarbonaceous oils, 2. Descri~ion of_he Prior Art 6 Hydrorefining is a well known process for 7 upgrading a variety of hydrs~carbon Eractions. The term 8 "hydrorefining" is used herein to designate a catalytic g treatment in the presence of hydrogen, of a hydro-10 carbonaceous oil, to upgrade the oil by eliminating or 11 reducing the concentration of contaminants in the oil 12 such as sulfur compounds, nitrogenous compounds, metal 3 contaminants and/or partial saturation of the oll.
14 U.S. Patents 3,953,321 and 4,098,721 disclose 15 a hydrodesulfurization process for heavy hydrocarbon-16 aceous oils such as gas oils in which a conventional 17 hydrodesulfurization catalyst is sulfided and heat 18 treated at a temperature of 750 to 850F prior to 19 initiating the hydrodesulfurization. The catalyst is 20 sulfided by contact with a lighter boiling range oil 21 (column 3, lines 59-68) or is heat treated in the 22 presence of the lighter oil~ free from sulfur (column 4, 23 lines 14-19).
24 U.S. Patent 2,954,339 discloses use of a 25 spent cobalt-molybdenum-alumina catalyst for hydrode-26 sulfurization of a hydrocarbonaceous oil which may be 27 a gas oil. Prior to contact with the gas oil, the 28 catalyst is used to hydrotreat naphtha.
29 Il.S. Patent 3,423 t 307 discloses a start-up 30 method for a hydrodesulfurization process for heavy ~Zt~'Y~:g6 1 residual feeds which contain asphaltic materials. The 2 catalyst is initially contacted with an asphaltic-free 3 feed.
4 U.S. Patent 3,528,910 discloses a hydrotreat-ing process for hydrocarbonaceous oils. A catalyst, 6 such as a supported nickel-molybdenum catalyst, is 7 sulfided in the presence of hydrogen with a distillate 8 containing disulfide sulfur prior to the hydrotreating g reaction.
U,S. Patent 4,149,965 discloses a start-up 11 process for hydrorefining of naphtha. The catalyst is 12 partially deactivated by treatment with a substantially 13 non-metal containing hydrocarbon oil in the presence 1~ f hydrogen prior to contacting the catalys~ with the naphtha feed.
16 U.S. Patent 3,368,965 discloses a slurry 17 hydrogenation process in which a catalyst, such as 18 cobalt molybdate on alumina, is pretreated by wetting 19 the catalyst with a clean (i.e. non-aromatic) hydro-carbonaceous oil such as a lubricating oil fraction 21 to form a slurry which is then introduced into the 22 hydrocarbonaceous oil to be hydrogenated.
23 It has now been ~ound that by pretreating a 24 sulfided hydrorefining catalyst with a light hydrocar-bonaceous oil in the presence of hydrogen prior to 26 hydrorefining the heavy hydrocarbonaceous oil feed, the 27 initial activity of the catalyst can be incr2ased.
28 All boiling points to which reference is made 29 herein are atmospheric boiling points unless otherwise specified.
l The Periodic Table referred to herein is 2 in accordance with Handbook of Chemistr~ and Physics, 3 published by the Chemical Rubber Company, Cleveland, 4 Ohio, 45th Edition, 1954.
14 U.S. Patents 3,953,321 and 4,098,721 disclose 15 a hydrodesulfurization process for heavy hydrocarbon-16 aceous oils such as gas oils in which a conventional 17 hydrodesulfurization catalyst is sulfided and heat 18 treated at a temperature of 750 to 850F prior to 19 initiating the hydrodesulfurization. The catalyst is 20 sulfided by contact with a lighter boiling range oil 21 (column 3, lines 59-68) or is heat treated in the 22 presence of the lighter oil~ free from sulfur (column 4, 23 lines 14-19).
24 U.S. Patent 2,954,339 discloses use of a 25 spent cobalt-molybdenum-alumina catalyst for hydrode-26 sulfurization of a hydrocarbonaceous oil which may be 27 a gas oil. Prior to contact with the gas oil, the 28 catalyst is used to hydrotreat naphtha.
29 Il.S. Patent 3,423 t 307 discloses a start-up 30 method for a hydrodesulfurization process for heavy ~Zt~'Y~:g6 1 residual feeds which contain asphaltic materials. The 2 catalyst is initially contacted with an asphaltic-free 3 feed.
4 U.S. Patent 3,528,910 discloses a hydrotreat-ing process for hydrocarbonaceous oils. A catalyst, 6 such as a supported nickel-molybdenum catalyst, is 7 sulfided in the presence of hydrogen with a distillate 8 containing disulfide sulfur prior to the hydrotreating g reaction.
U,S. Patent 4,149,965 discloses a start-up 11 process for hydrorefining of naphtha. The catalyst is 12 partially deactivated by treatment with a substantially 13 non-metal containing hydrocarbon oil in the presence 1~ f hydrogen prior to contacting the catalys~ with the naphtha feed.
16 U.S. Patent 3,368,965 discloses a slurry 17 hydrogenation process in which a catalyst, such as 18 cobalt molybdate on alumina, is pretreated by wetting 19 the catalyst with a clean (i.e. non-aromatic) hydro-carbonaceous oil such as a lubricating oil fraction 21 to form a slurry which is then introduced into the 22 hydrocarbonaceous oil to be hydrogenated.
23 It has now been ~ound that by pretreating a 24 sulfided hydrorefining catalyst with a light hydrocar-bonaceous oil in the presence of hydrogen prior to 26 hydrorefining the heavy hydrocarbonaceous oil feed, the 27 initial activity of the catalyst can be incr2ased.
28 All boiling points to which reference is made 29 herein are atmospheric boiling points unless otherwise specified.
l The Periodic Table referred to herein is 2 in accordance with Handbook of Chemistr~ and Physics, 3 published by the Chemical Rubber Company, Cleveland, 4 Ohio, 45th Edition, 1954.
5 SUMMARY OF T~IE INVENTION
6 In accordance wi~h the invention there is
7 provided, in a hydrorèfining process which comprises
8 contacting a heavy hydrocarbonaceous oil having a g boiling point ranging from about 650F to about 1050F
with hydrogen in the presence of a. sulfided hydro-11 refining catalyst comprising a hydrogenation component 12 sel~cted from the group consisting of Group VIB metal 13 components and Group VIII non-noble metal components 14 and an alumina-containing support, at hydrorefining conditions, the improvement which comprises initially 16 contacting said sulfided catalyst with a hydrocarbon-17 aceous oil lighter than said heavy oil feed~ in the 18 presence of hydrogen, at a temperature ran~ing from 19 about 500 ~o about 725F, for at least 2 days, and subsequently contacting said catalyst with said heavy 21 oil at said hydrorefining conditions.
23 The igu~e shows graphs of catalyst activi~y 24 versus days on oil.
DETAILED DESCRIPTION OF THE INVENTION
26 The start-up method of the present invention is 27 suited for use at the beginning of a process for hydro-28 refining heavy hydrocarbonaceous oil feeds utilizing a 29 hydrorefining catalyst that has already been sulfided in a conventional manner. The sulfided hydrorefining ,~,%~t~Gg~
1 catalyst is contacted with a hydrocarbonaceous oil 2 lighter than the hydrocarbonaceous oil feed which is to 3 be hydrorefined, at conditions shown in Table I.
LIGHT OIL TREATMENT CONDITIONS
~ Conditions Broad Range Preferred Ran~e 7 Temperature, F 500-750 600-700 8 Pressure, psig 500-3500 800-3000 g Liquid hourly space 10 velocity, V/HR/V 0.05-5.0 0.1-300 11 ~Iydrogen Rate, SCF/B 300-20,000 600-12,000 12 Hydrogen Partial 13 Pressure, psig 500-3500 650-2500 14 Suitable hydrorefining catalysts for use in the process comprise a hydrogenation componen~ and an 16 alumina-containing support. The hydrogenation component 17 is selected from the group consisting of Group VIB metal 18 component and a non-noble Group VIII metal components 19 and mixtures thereof, such as cobalt, molybdenum, nickel, tungsten and mixtures thereof. The alumina-21 ~ontaining support may comprise a minor amount of ~22 another inorganic oxide such as siIica, magnesia, boria, 23 zirconia, strontia, hafnia, phosphorous oxide and 2~ mixtures thereofO Preferably, the support is an alumina-containing support which additionally comprises minor 26 amounts of silica, such as for example from 1 to 6 27 percent silica, based on the weight of the support.
28 Such catalysts are described, for example, in U.S.
29 Patents 3,770,618 and 3,509,044 and 4,113,656~ The preferred catalyst comprises molybdenum and cobalt or 31 nickel on an alumina support containing from 1 to 6 .
:
'7~
1 percent silica, based on the support. The hydrogenation 2 component of the catalyst may initiaily be present as 3 elemental metal, metal oxide, metal sulfide and mixtures 4 thereof of the stated metals. When the initial hydro-5 genation component is not in the sulfided state, then 6 the catalyst, e.g. the nickel oxide-containing catalyst, 7 is sulfided in a conventional manner well-known in the 8 art prior to the contacting step of the present inven-g tion with the light hydrocarbon oil~ Suitable lighter hydrocarbon oils for initial contact with the already 11 sulfided catalyst include hydrocarbonaceous oils having 12 an at~ospheric pressure boiling point not greater than 13 about 700F, preferably a boiling point ranging from 14 about Cs to not greater than about 700F. The contact-ing with the lighter oil is conducted for at least 2 16 days. After the catalyst has been contacted with a 17 light oil, for the required time, in the presence of 18 hydrogen and at the above given conditions, the catalyst 19 i5 contacted with a heavy oil feed to be hydrorefined at hydrorefining conditions. The contact of the light oil 21 ~ay be discontinued prior to contacting immediately 22 with the heavy oil or the heavy oil may be gradually 23 contacted with the catalyst while there is still some 24 light oil present. When the heavy oil is contacted with the catalyst while the light oil is still present, the 26 contact with the light oil is continued, preferably for 27 at least a time sufficient for the sulfur concentration 28 in the hydrorefined oil product~ under the given operat-29 ing conditions to be approximately constant (that is, a period at least sufficient to obtain a line-out of 31 product sulfur concentration). Eventually, the Elow of 32 light oil to contact the catalyst is discontinued~ It should also be noted that a hydrogen-containing gas is 34 being introduced into the hydrorefining zone during the light oil pretreatment of the catalyst as well as during 36 the hydrorefining reaction stage. The contacting of `` 1~0~6~36 1 the heavy oil feed with the catalyst is performed 2 im~ediately after the contacting of the catalyst with 3 a light oil without any intervening treatment steps 4 such as heat treating steps. Sui~able heavy oil feeds to be hydrore~ined include oils which are substantially 6 asphaltene-free and which boil in the range of about 7 6S0F to about 1050F at atmospheric pressure, such as 8 gas oils. The hydrocarbonaceous oîls may be derived g from any source such as tar sand oils, shale oil, liquids derived from coal liquefaction processes and 11 mixtures thereof. The oils to be hydrorefined comprise 12 at least 0.25 weight percent sulfur and may comprise up 13 to 8 weight percent sulfur and may additionally comprise 14 up to 4 weight percent nitrogen usually present as organic sulfur compounds and organic nitrogen compounds.
16 Suitable operating conditions in the hydro-17 refining zone are summarized in Table II.
20 Conditions ~ Preferred Ranqe 21 Temperature, F 600-900 650-850 22 Pressure, psig 600-3500 800 3200 23 Liquid hourly space 0.0S-5.0 0.1-2.5 24 velocity~ V/V/HR
25 Hydrogen rate, SCF/BBL 300-20,000 600-12,000 26 Hydrogen partial 500-3000 800-2500 27 pressure, psig 28 The catalyst may be disposed in the hydro-29 refining reaction zone as a fixed bed, moving b~d, 30 dispersed phase, fluidized bed, ebullating bed or a 31 slurry. The process of the present invention is par-32 ticularly suited for use in fixed bed processes~
:
1 Contact of the heavy oil feed in the presence of hydro-2 gen and the catalyst at hydrorefining conditions pro-3 duces a hydrorefined heavy oil having a decreased 4 content of sulfur and nitrogen contaminants~
PREFERRED EMBODIMENT
6 The following example is presented to illus-7 trate the invention.
with hydrogen in the presence of a. sulfided hydro-11 refining catalyst comprising a hydrogenation component 12 sel~cted from the group consisting of Group VIB metal 13 components and Group VIII non-noble metal components 14 and an alumina-containing support, at hydrorefining conditions, the improvement which comprises initially 16 contacting said sulfided catalyst with a hydrocarbon-17 aceous oil lighter than said heavy oil feed~ in the 18 presence of hydrogen, at a temperature ran~ing from 19 about 500 ~o about 725F, for at least 2 days, and subsequently contacting said catalyst with said heavy 21 oil at said hydrorefining conditions.
23 The igu~e shows graphs of catalyst activi~y 24 versus days on oil.
DETAILED DESCRIPTION OF THE INVENTION
26 The start-up method of the present invention is 27 suited for use at the beginning of a process for hydro-28 refining heavy hydrocarbonaceous oil feeds utilizing a 29 hydrorefining catalyst that has already been sulfided in a conventional manner. The sulfided hydrorefining ,~,%~t~Gg~
1 catalyst is contacted with a hydrocarbonaceous oil 2 lighter than the hydrocarbonaceous oil feed which is to 3 be hydrorefined, at conditions shown in Table I.
LIGHT OIL TREATMENT CONDITIONS
~ Conditions Broad Range Preferred Ran~e 7 Temperature, F 500-750 600-700 8 Pressure, psig 500-3500 800-3000 g Liquid hourly space 10 velocity, V/HR/V 0.05-5.0 0.1-300 11 ~Iydrogen Rate, SCF/B 300-20,000 600-12,000 12 Hydrogen Partial 13 Pressure, psig 500-3500 650-2500 14 Suitable hydrorefining catalysts for use in the process comprise a hydrogenation componen~ and an 16 alumina-containing support. The hydrogenation component 17 is selected from the group consisting of Group VIB metal 18 component and a non-noble Group VIII metal components 19 and mixtures thereof, such as cobalt, molybdenum, nickel, tungsten and mixtures thereof. The alumina-21 ~ontaining support may comprise a minor amount of ~22 another inorganic oxide such as siIica, magnesia, boria, 23 zirconia, strontia, hafnia, phosphorous oxide and 2~ mixtures thereofO Preferably, the support is an alumina-containing support which additionally comprises minor 26 amounts of silica, such as for example from 1 to 6 27 percent silica, based on the weight of the support.
28 Such catalysts are described, for example, in U.S.
29 Patents 3,770,618 and 3,509,044 and 4,113,656~ The preferred catalyst comprises molybdenum and cobalt or 31 nickel on an alumina support containing from 1 to 6 .
:
'7~
1 percent silica, based on the support. The hydrogenation 2 component of the catalyst may initiaily be present as 3 elemental metal, metal oxide, metal sulfide and mixtures 4 thereof of the stated metals. When the initial hydro-5 genation component is not in the sulfided state, then 6 the catalyst, e.g. the nickel oxide-containing catalyst, 7 is sulfided in a conventional manner well-known in the 8 art prior to the contacting step of the present inven-g tion with the light hydrocarbon oil~ Suitable lighter hydrocarbon oils for initial contact with the already 11 sulfided catalyst include hydrocarbonaceous oils having 12 an at~ospheric pressure boiling point not greater than 13 about 700F, preferably a boiling point ranging from 14 about Cs to not greater than about 700F. The contact-ing with the lighter oil is conducted for at least 2 16 days. After the catalyst has been contacted with a 17 light oil, for the required time, in the presence of 18 hydrogen and at the above given conditions, the catalyst 19 i5 contacted with a heavy oil feed to be hydrorefined at hydrorefining conditions. The contact of the light oil 21 ~ay be discontinued prior to contacting immediately 22 with the heavy oil or the heavy oil may be gradually 23 contacted with the catalyst while there is still some 24 light oil present. When the heavy oil is contacted with the catalyst while the light oil is still present, the 26 contact with the light oil is continued, preferably for 27 at least a time sufficient for the sulfur concentration 28 in the hydrorefined oil product~ under the given operat-29 ing conditions to be approximately constant (that is, a period at least sufficient to obtain a line-out of 31 product sulfur concentration). Eventually, the Elow of 32 light oil to contact the catalyst is discontinued~ It should also be noted that a hydrogen-containing gas is 34 being introduced into the hydrorefining zone during the light oil pretreatment of the catalyst as well as during 36 the hydrorefining reaction stage. The contacting of `` 1~0~6~36 1 the heavy oil feed with the catalyst is performed 2 im~ediately after the contacting of the catalyst with 3 a light oil without any intervening treatment steps 4 such as heat treating steps. Sui~able heavy oil feeds to be hydrore~ined include oils which are substantially 6 asphaltene-free and which boil in the range of about 7 6S0F to about 1050F at atmospheric pressure, such as 8 gas oils. The hydrocarbonaceous oîls may be derived g from any source such as tar sand oils, shale oil, liquids derived from coal liquefaction processes and 11 mixtures thereof. The oils to be hydrorefined comprise 12 at least 0.25 weight percent sulfur and may comprise up 13 to 8 weight percent sulfur and may additionally comprise 14 up to 4 weight percent nitrogen usually present as organic sulfur compounds and organic nitrogen compounds.
16 Suitable operating conditions in the hydro-17 refining zone are summarized in Table II.
20 Conditions ~ Preferred Ranqe 21 Temperature, F 600-900 650-850 22 Pressure, psig 600-3500 800 3200 23 Liquid hourly space 0.0S-5.0 0.1-2.5 24 velocity~ V/V/HR
25 Hydrogen rate, SCF/BBL 300-20,000 600-12,000 26 Hydrogen partial 500-3000 800-2500 27 pressure, psig 28 The catalyst may be disposed in the hydro-29 refining reaction zone as a fixed bed, moving b~d, 30 dispersed phase, fluidized bed, ebullating bed or a 31 slurry. The process of the present invention is par-32 ticularly suited for use in fixed bed processes~
:
1 Contact of the heavy oil feed in the presence of hydro-2 gen and the catalyst at hydrorefining conditions pro-3 duces a hydrorefined heavy oil having a decreased 4 content of sulfur and nitrogen contaminants~
PREFERRED EMBODIMENT
6 The following example is presented to illus-7 trate the invention.
9 Comparative hydrorefining runs were made utilizing the start-up procedure of the present inven-11 tion and conventional start-up procedures. The catalyst 12 used in all the runs was the same catalyst, that is, 13 a conventional nickel-molybdenum-alumina catalyst 14 containing about 3 percent nickel r calculated as nickel oxide, and about 15 percent molybd~num, calculated as 16 molybdenum oxide~ The catalyst was sulfided in the 17 conventional manner by contact with a blend of 10 volume 18 percent hydrogen sulfide and hydrogen. The feed used 19 in the hydrorefining runs was the same heavy hydrocar-bonaceous oil feed having a boiling point ranging from 21 about 650 to about 1050F, a sulfur content of 2.3 22 wei~ht percent and a nitrogen content of 0.1 weight 23 percent. The feed was substantially free of asphaltenes 24 In runs A and B, which simulate a conventional start-up procedure, the heavy oil was introduced into 26 the reaction zone immediately after the catalyst had 27 been sulfided. In runs C and D, which are runs in 28 accordance with the start-up procedure of the present 29 inven~ion, the sulfided catalyst was contacted with a light hydrocarbonaceous oil having a boiling point 31 ranging from Cs to 700F in the presence of hydrogen , ., 7~
1 for about 30 to about 40 days at the conditions given in 2 Table III prior to introducing the heavy oil to be 3 hydrorefined into the hydrorefining zone.
4 The light oil treatment conditions used in Runs C and D are summarized in Table III~
8 Conditions ~ Run CRun D
g Temperature, F 629-662630
1 for about 30 to about 40 days at the conditions given in 2 Table III prior to introducing the heavy oil to be 3 hydrorefined into the hydrorefining zone.
4 The light oil treatment conditions used in Runs C and D are summarized in Table III~
8 Conditions ~ Run CRun D
g Temperature, F 629-662630
10 Hydrogen pressure, psig 1200 1200
11 Liquid hourly space
12 velocity, V/HR/V 0.3-1~0 0~5
13 Hydrogen Rate, SCF/B 3000 3000
14 The hydrorefining conditions and ~esults of these runs are summarized in Table IV.
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~0'~ 6 l The hydrodesulfurization and hydrodenitrogena-2 tion activities of the catalyst in runs A, B, C and D, 3 that is, without light oil treatment and with light oil 4 treatment, versus days on oil is shown in the four graphs in the accompanying figure.
6 As can be seen from Table IV, runs C and D
7 showed increased catalyst activity. The increased 8 activity can be used to decrease the catalyst require-9 ment or to decrease the start o the run temperature7 As can be seen from the figure, the hydro-ll denitrogenation and hydrodesulfurization rate cons~a,nts 12 of the catalyst in runs C and D (runs in accordance with 13 the present invention) were lined out and the catalyst 14 maintained a higher level of activity than the catalyst of runs A and B, which had not been treated in accord-16 ance with the present invention.
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~0'~ 6 l The hydrodesulfurization and hydrodenitrogena-2 tion activities of the catalyst in runs A, B, C and D, 3 that is, without light oil treatment and with light oil 4 treatment, versus days on oil is shown in the four graphs in the accompanying figure.
6 As can be seen from Table IV, runs C and D
7 showed increased catalyst activity. The increased 8 activity can be used to decrease the catalyst require-9 ment or to decrease the start o the run temperature7 As can be seen from the figure, the hydro-ll denitrogenation and hydrodesulfurization rate cons~a,nts 12 of the catalyst in runs C and D (runs in accordance with 13 the present invention) were lined out and the catalyst 14 maintained a higher level of activity than the catalyst of runs A and B, which had not been treated in accord-16 ance with the present invention.
:
Claims (10)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A hydrorefining process which comprises contacting a heavy hydrocarbonaceous oil feed having a boiling point ranging from about 650 to about 1050°F
with hydrogen in the presence of a sulfided hydrorefin-ing catalyst comprising a hydrogenation component selected from the group consisting of Group VIB metal component, Group VIII non-noble metal component and mixtures thereof, and an alumina-containing support, at hydrorefining conditions, characterized in that the improvement which comprises initially contacting the sulfided catalyst with a hydrocarbonaceous oil lighter than said heavy oil feed, in the presence of hydrogen at a temperature ranging from about 500 to about 750°F, for at least 2 days, and subsequently contacting said catalyst with said heavy oil feed at said hydrorefining conditions.
with hydrogen in the presence of a sulfided hydrorefin-ing catalyst comprising a hydrogenation component selected from the group consisting of Group VIB metal component, Group VIII non-noble metal component and mixtures thereof, and an alumina-containing support, at hydrorefining conditions, characterized in that the improvement which comprises initially contacting the sulfided catalyst with a hydrocarbonaceous oil lighter than said heavy oil feed, in the presence of hydrogen at a temperature ranging from about 500 to about 750°F, for at least 2 days, and subsequently contacting said catalyst with said heavy oil feed at said hydrorefining conditions.
2. The process of claim 1 wherein said sulfided catalyst is contacted with said lighter oil at a temperature ranging from about 600 to about 700°F.
3. The process of claim 1 wherein said lighter oil has a boiling point ranging from about C5 to a final boiling point not greater than about 700°F.
4. The process of claim 1 wherein said heavy oil feed is a substantially asphaltene-free oil.
5. The process of claim 1 wherein said heavy oil feed comprises from about 0.25 to about 8 weight percent sulfur.
6. The process of claim 1 wherein said hydrorefining conditions include a temperature ranging from about 600 to 900°F and a pressure ranging from about 600 to about 3500 psig.
7. The process of claim 1 wherein said hydrogenation component comprises a metal selected from the group consisting of nickel, cobalt, molybdenum, tungsten, and mixtures thereof.
8. The process of claim 1 wherein said support comprises alumina and additionally comprises a minor amount of silica.
9. The process of claim 1 wherein said initial contacting of said catalyst with said light oil and said subsequent contacting with said heavy oil feed are performed without any intervening treatment steps.
10. A method for starting up a hydrorefining process for a heavy hydrocarbonaceous oil feed, which comprises:
(a) contacting a sulfided hydrorefining catalyst comprising a hydrogenation component selected from the group consisting of at least one Group VIB
metal component and at least one non-noble metal Group VIII metal component and an alumina-containing support with a hydrocarbonaceous oil lighter than said feed, said lighter hydrocarbonaceous oil having a boiling point ranging from about C5 to not greater than about 700°F, in the presence of hydrogen, at a temperature ranging from about 600 to about 700°F and a pressure ranging from about 800 to about 3000 psig, for at least 2 days, and (b) contacting the catalyst resulting from step (a) with a substantially asphaltene-free heavy hydrocarbonaceous oil feed boiling in the range of about 650 to about 1050°F in the presence of hydrogen at hydrorefining conditions, and (c) recovering a hydrorefined heavy hydrocar-bonaceous oil.
(a) contacting a sulfided hydrorefining catalyst comprising a hydrogenation component selected from the group consisting of at least one Group VIB
metal component and at least one non-noble metal Group VIII metal component and an alumina-containing support with a hydrocarbonaceous oil lighter than said feed, said lighter hydrocarbonaceous oil having a boiling point ranging from about C5 to not greater than about 700°F, in the presence of hydrogen, at a temperature ranging from about 600 to about 700°F and a pressure ranging from about 800 to about 3000 psig, for at least 2 days, and (b) contacting the catalyst resulting from step (a) with a substantially asphaltene-free heavy hydrocarbonaceous oil feed boiling in the range of about 650 to about 1050°F in the presence of hydrogen at hydrorefining conditions, and (c) recovering a hydrorefined heavy hydrocar-bonaceous oil.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/463,398 US4485006A (en) | 1982-03-04 | 1983-02-03 | Start-up method for a hydrorefining process |
| US463,398 | 1983-02-03 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1207696A true CA1207696A (en) | 1986-07-15 |
Family
ID=23839942
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000445234A Expired CA1207696A (en) | 1983-02-03 | 1984-01-13 | Start-up method for a hydrorefining process |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1207696A (en) |
-
1984
- 1984-01-13 CA CA000445234A patent/CA1207696A/en not_active Expired
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