CA2043403A1 - Resid desulfurization and demetalation - Google Patents
Resid desulfurization and demetalationInfo
- Publication number
- CA2043403A1 CA2043403A1 CA 2043403 CA2043403A CA2043403A1 CA 2043403 A1 CA2043403 A1 CA 2043403A1 CA 2043403 CA2043403 CA 2043403 CA 2043403 A CA2043403 A CA 2043403A CA 2043403 A1 CA2043403 A1 CA 2043403A1
- Authority
- CA
- Canada
- Prior art keywords
- resid
- demetalation
- alumina
- silica
- desulfurization
- 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.)
- Abandoned
Links
- 238000007324 demetalation reaction Methods 0.000 title claims abstract description 14
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 18
- 230000023556 desulfurization Effects 0.000 title abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 14
- 238000009835 boiling Methods 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims abstract 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 19
- 239000003085 diluting agent Substances 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 16
- 239000003921 oil Substances 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 9
- 229910052759 nickel Inorganic materials 0.000 claims description 9
- 229910052720 vanadium Inorganic materials 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 239000000377 silicon dioxide Substances 0.000 claims description 4
- 239000002574 poison Substances 0.000 claims description 3
- 231100000614 poison Toxicity 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 claims 1
- 238000011143 downstream manufacturing Methods 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052717 sulfur Inorganic materials 0.000 abstract description 12
- 239000011593 sulfur Substances 0.000 abstract description 12
- 229910052751 metal Inorganic materials 0.000 abstract description 7
- 239000002184 metal Substances 0.000 abstract description 7
- 150000002739 metals Chemical class 0.000 abstract description 5
- 239000003208 petroleum Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 description 10
- 125000003118 aryl group Chemical group 0.000 description 3
- 239000000356 contaminant Substances 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000003350 kerosene Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005292 vacuum distillation Methods 0.000 description 2
- -1 Ni and V Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
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
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
RESID DESULFURIZATION AND DEMETALATION
ABSTRACT
This invention relates to improved processes for hydrotreating resid. Blending lower boiling petroleum fractions with the resid results in enhanced rates of demetalation and/or desulfurization, with enhanced reduction of sulfur and/or metals content in the hydroprocessed resid.
ABSTRACT
This invention relates to improved processes for hydrotreating resid. Blending lower boiling petroleum fractions with the resid results in enhanced rates of demetalation and/or desulfurization, with enhanced reduction of sulfur and/or metals content in the hydroprocessed resid.
Description
RESID DESULFURIZATION AND DEMETALATION
This invention relates to improved demetalation and desulfurization of resids, e.g. vacuum resids. In accordance with the invention, demetalation and/or desulfurization are undertaken to substantially reduce or remove contaminants from the resid. The contaminants would interfere with catalysts, for example as poisons, in subsequent catalytic processing of the resid such as in the production of gasoline.
The invention relates to contacting a resid with gas oil, a distillate, or FCC cycle stock diluent, under conditions includinq hydrogen pressures ranging from 4240 to 27,700 kPa (600 to 4000 psig); space velocities (WHSV) from 0 .05 to l0, and temperatures ranging from 316 to 468C (600 to 875F) over a catalyst comprising silica, alumina or silica-alumina.
One result is that the metal contaminant content of the treated resid is less than that of the resid treated under identical conditions in the absence of the gas oil, distillate, or FCC cycle stock. Another result is that the sulfur content of the resid treated in the presence of those lower boiling fractions (gas oil, distillate or FCC cycle stock) under the conditions is less than that of the resid treated under identical conditions in the absence of the gas oil, distillate, or FCC cycle stock.
Figure l is a plot of the fraction of ~nickel in the product)/~nickel in the feed) V9. WHSV and illustrates the effect of light cycle oil (LCO) on Nickel removal.
Figure 2, wherein the fraction of (vanadium in the product)/(vanadium in the feed) is plotted against WHSV
illustrates the effect of LCO on vanadium removal.
This invention relates to improved demetalation and desulfurization of resids, e.g. vacuum resids. In accordance with the invention, demetalation and/or desulfurization are undertaken to substantially reduce or remove contaminants from the resid. The contaminants would interfere with catalysts, for example as poisons, in subsequent catalytic processing of the resid such as in the production of gasoline.
The invention relates to contacting a resid with gas oil, a distillate, or FCC cycle stock diluent, under conditions includinq hydrogen pressures ranging from 4240 to 27,700 kPa (600 to 4000 psig); space velocities (WHSV) from 0 .05 to l0, and temperatures ranging from 316 to 468C (600 to 875F) over a catalyst comprising silica, alumina or silica-alumina.
One result is that the metal contaminant content of the treated resid is less than that of the resid treated under identical conditions in the absence of the gas oil, distillate, or FCC cycle stock. Another result is that the sulfur content of the resid treated in the presence of those lower boiling fractions (gas oil, distillate or FCC cycle stock) under the conditions is less than that of the resid treated under identical conditions in the absence of the gas oil, distillate, or FCC cycle stock.
Figure l is a plot of the fraction of ~nickel in the product)/~nickel in the feed) V9. WHSV and illustrates the effect of light cycle oil (LCO) on Nickel removal.
Figure 2, wherein the fraction of (vanadium in the product)/(vanadium in the feed) is plotted against WHSV
illustrates the effect of LCO on vanadium removal.
2~43~03 Figure 3 illustrates the effect of LC0 on resid desulfurization, wherein the change in sulfur in the resid is plotted against WHSV
Figure 4 is a plot of nickel vs. WHSV and shows the effect of diluent on demetalation of 8So+ bottom.
Figure 5 is a plot of vanadium vs. WHSV and illustrates the effect of diluent on demetalation of 850+ bottom.
Figure 6 is a plot of sulfur vs. WHSV and illustrates the effect of diluent on desulfurization of 850+ bottom.
The objective of hydrotreating resids is to remove metals such as Ni and V, reduce product S, and reduce product CCR. Kinetic limitations and catalyst fouling by carbonaceous deposits and metal deposits are two common problems encountered in such processing.
Atmospheric resids boil above 316 to 427C (6000 to 800F), while vacuum resids boil above 482 up to 593C
(9ooo up to about 1100F). Preferably, the resid which is subjected to demetalation and/or desulfurization, in accordance with the invention, is a vacuum resid.
Resids are, by definition, the unevaporated liquid or solid bottoms from processes of distillation or cracking of petroleum crudes. Vacuum resids result from vacuum distillation which is undertaken, under reduced pressure, to reduce the distillation temperature and the boiling temperature of the distilled material to prevent decomposition and cracking of the material being distilled. Accordingly, in preferred embodiments of the process the first stage is providing a vacuum resid; this involves previousl undertaking is a vacuum distillation of petroleum crude to provide the vacuum resid, by standard methods.
Lower boiling diluents for the resid include `
atmospheric and vacuum gas oils, or cracked distillates such as LC0 (light cycle oil) and HC0 (heavy cycle 204340~
oil). Gas oil is a petroleum distillate with a viscosity intermediate between kerosene and lubricating oil, boiling in the range of 204 to 427C (about 4000 to about 800F). Distillate includes gasoline, s kerosene and light lubrication oil. In a preferred embodiment, the diluent is an aromatic stream such as cracked FCC distillate. Cracked distillate, as an aromatic stream, includes LCO and HCO. Combination of the resid with the aromatic stream provided by cracked distillate, in the process of the invention, results in a beneficial impact on catalyst deactivation.
The resid is blended with the lower boiling diluent. The resulting blend can contain up to 50 volume percent of the diluent. Practically, the blend will contain about lo to 30 volume percent of the diluent. Optimum levels of dilution are determined for each combination of vacuum resid and diluent: optimum levels of dilution are amounts of diluents lower boiling than the resid effective to increase the dematalation and desulfurization of the resid under the hydroprocessing conditions reported below. In accordance with the invention, rate enhancement, of either or both demetalation and desulfurization, can be up to one hundred percent (100%). At one hundred percent rate enhancement with a specific diluent, rate enhancement will tend to be greater as the viscosity of the resid to be treated.
The viscosity of the resid will vary with its source.
The blend of resid and diluent can be subje¢ted to the following hydroprocessing conditions in fixed-, ebullated-, or moving-bed reactors that are well known in the art for dematalation and desulfurization of petroleum resids. The hydroprocessing conditions include a catalyst.
By definition, hydroprocessing requires a hydrogen stream. The hydrogen pressures, in the process of the - 204340~
F-5771 - 4 ~
invention, range from 4240 to 27,700 kPa (600 to about 4000 psig). Elevated temperatures in the process of the invention range from about 316 to 468C (600F to about 875F). Space velocities (WHSV) range from 0.05 to 10.
The catalyst for resid demetalation and/or desulfurization can be a conventional one. Those compositions useful as catalysts include silica, alumina or silica-alumina.
Under the foregoing conditions, the rate constants for dematalation and/or desulfurization of resid hydroprocessed in the presence of said lower boiling diluent is enhanced. The extent of this enhancement allows a certain proportion of diluent to be hydrotreated in the same reactor with no negative consequence and even a positive effect on the treatment of the vacuum resid fraction.
The product of this process can be optionally fractionated and set to other conversion units or used directly as a finished product.
The invention has been illustrated above with respect to specific embodiments thereof. However, the invention will be defined by the claims appended hereto which are intended to embrace modifications within the skill of the art.
EXAMPLES
Example l An Arab Light (AL) vacuum resid was hydrotreated in the presence of 30% LC0 at a variety of space velocities. Fig. 1 shows the effect of the LC0 on the rate constant for Ni removal and Figure 2 shows the effect on V removal. The presence of 30% LC0 enhances demetalation by more than a factor of two as measured by improvement of rate constants. For example, at 371C (700F) and 13,900 kPa (2000 psig) with 890 v/v (5000 SCF/BBL) hydrogen circulation, the calculated :
.
.
20~3403 apparent rate constants for nickel removal is 0.022 when processsing the resid alone. The rate constant increases to 0.045 when 30% LCO is coprocessed.
Similarly, the rate constant for vanadium removal is increased from 0.021 to 0.05 when 30% LCO is coprocessed. This improved demetalation rate translates to lower metals content in the product.
ExamPle 2 An AL vacuum resid was hydrotreated in the presence of 30% LC0. Sulfur in the resid fraction is calculated by backing out the residual sulfur in the LC0 fraction after the treatment. In Figure 3, the observed desulfurization of vacuum resid in coprocessing is compared with the expected desulfurization when processing vacuum resid by itself.
Again, at the same operating condition as in Example 1, the rate constant for desulfurization is increased from 0.2 to 0.36 by coprocessing. This translates to significantly lower sulfur content in the product stream.
Example 3 To isolate the effects of LC0 on catalyst deactivation, LCO was processed by itself for four days on an equilibrated catalyst at the same condition as in Example 1. Catalyst performance on resid hydrotreatment is compared before and after LC0 runs.
As shown below, metals removal from AL resid was incraased from 43 to 46%, while sulfur removal was increased from 38 to 41%.
20~3~03 Com~arison of HDT on Resid Feed Before After Operating Conditions P, kPa 13,400 13,400 (psig) (2,000)(2,000) T, ~ 321 321 (F) (610) (610) WHSV 0.8 0.8 Product Properties Ni, ppm 9.0 6.9 6.5 V, 31.0 16.0 15.0 S, wt% 2.9 0.9 0.75 Dematalation ~ 43 46 Desulfurization, % 38 41 The foregoing indicates that the presence of LCO
actually restores catalytic activity. Therefore, coprocessing LCO is expected to slow catalyst deactivation.
Example 4 An AL vacuum resid was coprocessed with 20% vacuum gas oil and 10% light distillate at 321 and 399C
(610 and 750F), and 13,900 kPa (2000 psig) with 890 v/v (5000 SCF/BBL) hydrogen circulation. In order to follow sulfur removal from the vacuum resid, the product was cut to generate the 850+ (F) portion of which sulfur was measured. In Figure 4, the effect of diluent addition on nickel removal from vacuum resid is compared at various reactor temperatures. Similar improvement on vanadium and sulfur removal from the resid by coprocessing is shown respectively in Figures 5 and 6. As shown, coprocessing gives a substantial improvement of metals and sulfur removals.
,~, . . ...
Figure 4 is a plot of nickel vs. WHSV and shows the effect of diluent on demetalation of 8So+ bottom.
Figure 5 is a plot of vanadium vs. WHSV and illustrates the effect of diluent on demetalation of 850+ bottom.
Figure 6 is a plot of sulfur vs. WHSV and illustrates the effect of diluent on desulfurization of 850+ bottom.
The objective of hydrotreating resids is to remove metals such as Ni and V, reduce product S, and reduce product CCR. Kinetic limitations and catalyst fouling by carbonaceous deposits and metal deposits are two common problems encountered in such processing.
Atmospheric resids boil above 316 to 427C (6000 to 800F), while vacuum resids boil above 482 up to 593C
(9ooo up to about 1100F). Preferably, the resid which is subjected to demetalation and/or desulfurization, in accordance with the invention, is a vacuum resid.
Resids are, by definition, the unevaporated liquid or solid bottoms from processes of distillation or cracking of petroleum crudes. Vacuum resids result from vacuum distillation which is undertaken, under reduced pressure, to reduce the distillation temperature and the boiling temperature of the distilled material to prevent decomposition and cracking of the material being distilled. Accordingly, in preferred embodiments of the process the first stage is providing a vacuum resid; this involves previousl undertaking is a vacuum distillation of petroleum crude to provide the vacuum resid, by standard methods.
Lower boiling diluents for the resid include `
atmospheric and vacuum gas oils, or cracked distillates such as LC0 (light cycle oil) and HC0 (heavy cycle 204340~
oil). Gas oil is a petroleum distillate with a viscosity intermediate between kerosene and lubricating oil, boiling in the range of 204 to 427C (about 4000 to about 800F). Distillate includes gasoline, s kerosene and light lubrication oil. In a preferred embodiment, the diluent is an aromatic stream such as cracked FCC distillate. Cracked distillate, as an aromatic stream, includes LCO and HCO. Combination of the resid with the aromatic stream provided by cracked distillate, in the process of the invention, results in a beneficial impact on catalyst deactivation.
The resid is blended with the lower boiling diluent. The resulting blend can contain up to 50 volume percent of the diluent. Practically, the blend will contain about lo to 30 volume percent of the diluent. Optimum levels of dilution are determined for each combination of vacuum resid and diluent: optimum levels of dilution are amounts of diluents lower boiling than the resid effective to increase the dematalation and desulfurization of the resid under the hydroprocessing conditions reported below. In accordance with the invention, rate enhancement, of either or both demetalation and desulfurization, can be up to one hundred percent (100%). At one hundred percent rate enhancement with a specific diluent, rate enhancement will tend to be greater as the viscosity of the resid to be treated.
The viscosity of the resid will vary with its source.
The blend of resid and diluent can be subje¢ted to the following hydroprocessing conditions in fixed-, ebullated-, or moving-bed reactors that are well known in the art for dematalation and desulfurization of petroleum resids. The hydroprocessing conditions include a catalyst.
By definition, hydroprocessing requires a hydrogen stream. The hydrogen pressures, in the process of the - 204340~
F-5771 - 4 ~
invention, range from 4240 to 27,700 kPa (600 to about 4000 psig). Elevated temperatures in the process of the invention range from about 316 to 468C (600F to about 875F). Space velocities (WHSV) range from 0.05 to 10.
The catalyst for resid demetalation and/or desulfurization can be a conventional one. Those compositions useful as catalysts include silica, alumina or silica-alumina.
Under the foregoing conditions, the rate constants for dematalation and/or desulfurization of resid hydroprocessed in the presence of said lower boiling diluent is enhanced. The extent of this enhancement allows a certain proportion of diluent to be hydrotreated in the same reactor with no negative consequence and even a positive effect on the treatment of the vacuum resid fraction.
The product of this process can be optionally fractionated and set to other conversion units or used directly as a finished product.
The invention has been illustrated above with respect to specific embodiments thereof. However, the invention will be defined by the claims appended hereto which are intended to embrace modifications within the skill of the art.
EXAMPLES
Example l An Arab Light (AL) vacuum resid was hydrotreated in the presence of 30% LC0 at a variety of space velocities. Fig. 1 shows the effect of the LC0 on the rate constant for Ni removal and Figure 2 shows the effect on V removal. The presence of 30% LC0 enhances demetalation by more than a factor of two as measured by improvement of rate constants. For example, at 371C (700F) and 13,900 kPa (2000 psig) with 890 v/v (5000 SCF/BBL) hydrogen circulation, the calculated :
.
.
20~3403 apparent rate constants for nickel removal is 0.022 when processsing the resid alone. The rate constant increases to 0.045 when 30% LCO is coprocessed.
Similarly, the rate constant for vanadium removal is increased from 0.021 to 0.05 when 30% LCO is coprocessed. This improved demetalation rate translates to lower metals content in the product.
ExamPle 2 An AL vacuum resid was hydrotreated in the presence of 30% LC0. Sulfur in the resid fraction is calculated by backing out the residual sulfur in the LC0 fraction after the treatment. In Figure 3, the observed desulfurization of vacuum resid in coprocessing is compared with the expected desulfurization when processing vacuum resid by itself.
Again, at the same operating condition as in Example 1, the rate constant for desulfurization is increased from 0.2 to 0.36 by coprocessing. This translates to significantly lower sulfur content in the product stream.
Example 3 To isolate the effects of LC0 on catalyst deactivation, LCO was processed by itself for four days on an equilibrated catalyst at the same condition as in Example 1. Catalyst performance on resid hydrotreatment is compared before and after LC0 runs.
As shown below, metals removal from AL resid was incraased from 43 to 46%, while sulfur removal was increased from 38 to 41%.
20~3~03 Com~arison of HDT on Resid Feed Before After Operating Conditions P, kPa 13,400 13,400 (psig) (2,000)(2,000) T, ~ 321 321 (F) (610) (610) WHSV 0.8 0.8 Product Properties Ni, ppm 9.0 6.9 6.5 V, 31.0 16.0 15.0 S, wt% 2.9 0.9 0.75 Dematalation ~ 43 46 Desulfurization, % 38 41 The foregoing indicates that the presence of LCO
actually restores catalytic activity. Therefore, coprocessing LCO is expected to slow catalyst deactivation.
Example 4 An AL vacuum resid was coprocessed with 20% vacuum gas oil and 10% light distillate at 321 and 399C
(610 and 750F), and 13,900 kPa (2000 psig) with 890 v/v (5000 SCF/BBL) hydrogen circulation. In order to follow sulfur removal from the vacuum resid, the product was cut to generate the 850+ (F) portion of which sulfur was measured. In Figure 4, the effect of diluent addition on nickel removal from vacuum resid is compared at various reactor temperatures. Similar improvement on vanadium and sulfur removal from the resid by coprocessing is shown respectively in Figures 5 and 6. As shown, coprocessing gives a substantial improvement of metals and sulfur removals.
,~, . . ...
Claims (7)
1. A process for desulfurizing and demetalation of a resid comprising:
blending the resid with a diluent having a boiling temperature ranging from 204°C up to less than the boiling temperature of the resid to form a blend in which the resid is the predominant component;
contacting the blend with a hydrotreating catalyst, under conditions including hydrogen pressures ranging from 4240 to 27,700 kPa elevated temperatures ranging from 316° to 468°C and a space velocity ranging from about 0.05 to about 10; and recovering the processed blend.
blending the resid with a diluent having a boiling temperature ranging from 204°C up to less than the boiling temperature of the resid to form a blend in which the resid is the predominant component;
contacting the blend with a hydrotreating catalyst, under conditions including hydrogen pressures ranging from 4240 to 27,700 kPa elevated temperatures ranging from 316° to 468°C and a space velocity ranging from about 0.05 to about 10; and recovering the processed blend.
2. The process of Claim 1 , wherein the diluent for the resid is selected from atmospheric gas oil, vacuum gas oils, and cracked distillate light cycle oil and heavy cycle oil.
3. The process of Claim 1 or 2 , wherein the hydrotreating catalyst is one selected from silica, alumina, and silica-alumina.
4. The process of Claim 1, 2, or 3 , wherein the resid is a vacuum resid.
5. The process of any one of the preceding claims wherein the resid contains an amount of nickel or vanadium effective to act as a catalyst poison in subsequent downstream processing.
6. The process of any one of the preceding claims wherein the amount of vanadium or nickel in the recovered blend is less than the amount effective to act as catalyst poison.
7. The process of any one of the preceding claims wherein the hydrotreating catalyst is one selected from silica, alumina, and silica-alumina.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US540,721 | 1983-10-11 | ||
| US54072190A | 1990-06-21 | 1990-06-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2043403A1 true CA2043403A1 (en) | 1991-12-22 |
Family
ID=24156649
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2043403 Abandoned CA2043403A1 (en) | 1990-06-21 | 1991-05-28 | Resid desulfurization and demetalation |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0462823B1 (en) |
| JP (1) | JPH04239094A (en) |
| AU (1) | AU644166B2 (en) |
| CA (1) | CA2043403A1 (en) |
| DE (1) | DE69101670T2 (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4711849B2 (en) * | 2006-02-21 | 2011-06-29 | Ｊｘ日鉱日石エネルギー株式会社 | Manufacturing method of fuel substrate |
| CN100366709C (en) * | 2006-04-17 | 2008-02-06 | 中国石油化工集团公司 | Combined process for processing heavy oil |
| RU2009146027A (en) * | 2007-07-24 | 2011-06-20 | Идемицу Козан Ко., Лтд. (JP) | METHOD FOR HYDRAULIC CLEANING OF HYDROCARBON OIL PRODUCTS |
| JP5563491B2 (en) * | 2011-01-14 | 2014-07-30 | 出光興産株式会社 | Method for hydrotreating heavy hydrocarbon oil |
| US8932451B2 (en) | 2011-08-31 | 2015-01-13 | Exxonmobil Research And Engineering Company | Integrated crude refining with reduced coke formation |
| CN103102986B (en) * | 2011-11-10 | 2015-05-13 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
| CN104927920B (en) * | 2014-03-21 | 2017-03-15 | 中国石油化工股份有限公司 | A kind of residuum coking method |
| EP3957705A1 (en) * | 2015-05-12 | 2022-02-23 | Ergon, Inc. | High performance process oil |
| WO2016183200A1 (en) | 2015-05-12 | 2016-11-17 | Ergon, Inc. | High performance process oil based on distilled aromatic extracts |
| CN106367113A (en) * | 2015-07-23 | 2017-02-01 | 中国石化扬子石油化工有限公司 | Residual oil hydrotreating method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB833705A (en) * | 1956-03-14 | 1960-04-27 | Exxon Research Engineering Co | Destructive hydrogenation of asphaltic hydrocarbons |
| US4548709A (en) * | 1983-04-29 | 1985-10-22 | Mobil Oil Corporation | Hydrotreating petroleum heavy ends in aromatic solvents with dual pore size distribution alumina catalyst |
| US4808289A (en) * | 1987-07-09 | 1989-02-28 | Amoco Corporation | Resid hydrotreating with high temperature flash drum recycle oil |
-
1991
- 1991-05-23 AU AU77279/91A patent/AU644166B2/en not_active Ceased
- 1991-05-28 CA CA 2043403 patent/CA2043403A1/en not_active Abandoned
- 1991-06-19 DE DE1991601670 patent/DE69101670T2/en not_active Expired - Fee Related
- 1991-06-19 EP EP19910305552 patent/EP0462823B1/en not_active Expired - Lifetime
- 1991-06-21 JP JP15029491A patent/JPH04239094A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| AU644166B2 (en) | 1993-12-02 |
| EP0462823A1 (en) | 1991-12-27 |
| AU7727991A (en) | 1992-01-02 |
| JPH04239094A (en) | 1992-08-26 |
| EP0462823B1 (en) | 1994-04-13 |
| DE69101670D1 (en) | 1994-05-19 |
| DE69101670T2 (en) | 1994-07-28 |
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