CN100448542C - Hydrogenation catalyst precuring method - Google Patents
Hydrogenation catalyst precuring method Download PDFInfo
- Publication number
- CN100448542C CN100448542C CNB200410050714XA CN200410050714A CN100448542C CN 100448542 C CN100448542 C CN 100448542C CN B200410050714X A CNB200410050714X A CN B200410050714XA CN 200410050714 A CN200410050714 A CN 200410050714A CN 100448542 C CN100448542 C CN 100448542C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- oil
- presulfurization
- sulphuration
- hydrogen
- 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.)
- Active
Links
Abstract
The present invention discloses a prevulcanization method of a hydrogenation catalyst, which comprises: vulcanized oil containing an additive agent and a vulcanizing agent contacts a hydrogenation catalyst in a conventional oxidation state to be prevulcanized under prevulcanization conditions in a hydrogen containing atmosphere. The following prevulcanization conditions are adopted: the temperature is from 100DEG C to 400DEG C, the contact time is from 0.1h to 24h, the hydrogen partial pressure is from 0.1MPa to 15MPa, the liquid-phase space velocity is from 0.1/h to 10/h, and the volume ratio of the hydrogen to the oil is from 50 to 2000. The method provided by the present invention, which is used for prevulcanizing the hydrogenation catalyst, can be used for obviously improving the activity of the catalyst.
Description
Technical field
The present invention relates to a kind of method for pre-sulphuration of hydrogenation catalyst, be particularly suitable for the interior pre-vulcanization process of device of Hydrobon catalyst, hydrotreating catalyst and hydrocracking catalyst.
Background technology
Hydrogenation catalyst comprises numerous species; as being the Hydrobon catalyst of purpose with desulfurization, denitrogenation; with desulfurization, denitrogenation, deolefination, take off the hydrotreating catalyst that aromatic hydrocarbons is purpose; with demetalization, colloid and other impurity is the hydrogenation protecting agent of purpose, to produce the hydrocracking catalyst etc. that fuel oil is purpose.These hydrogenation catalysts generally are made up of carrier and the reactive metal that loads on this carrier, and wherein reactive metal is group vib and/or group VIII metal.Group vib metal commonly used is molybdenum and/or tungsten, and group VIII metal commonly used is nickel and/or cobalt.The carrier of Hydrobon catalyst, hydrogenation protecting agent generally is selected from heat-resistant inorganic oxide.The carrier of hydrocracking catalyst generally is selected from a kind of carrier that contains zeolite and heat-resistant inorganic oxide.The carrier of hydrotreating catalyst both can be heat-resistant inorganic oxide, also can be the mixture of zeolite and heat-resistant inorganic oxide.
Group vib reactive metal in the hydrogenation catalyst, as molybdenum and/or tungsten, the group VIII hydrogenation active metals is as nickel and/or cobalt, before use, all the form with oxidation state is present in the catalyst, in hydroconversion process, though owing to contain sulfide in the raw material, can be converted into sulphided state by reaction, but because under reaction condition, sulfur content is low excessively in the raw material, sulfur-containing compound structure more complicated, and sulfuration is not exclusively, cause a part of metallic reducing even make catalyst poisoning, make catalyst activity not reach normal level, therefore, in actual use, before carrying out hydroconversion reactions, need carry out presulfurization to hydrogenation catalyst.
The method of hydrogenation presulfurization can be divided into two big classes substantially, i.e. the outer presulfurization method of presulfurization and device in the device.The presulfurization method is a kind of traditional method for pre-sulphuration in the device, and it comprises gas phase presulfurization method and liquid phase presulfurization method (being the wet method presulfurization) again.The presulfurization method has been conventionally known to one of skill in the art in the device, to this, " Chinese oil Refining Technologies ", and the Hou Xianglin chief editor, Sinopec publishing house, 279-281,1991, done comparatively detailed summary.
The outer presulfurization method of device has also had many reports.For example US4177136 discloses a kind of method of vulcanizing hydrogenation catalyst, under the condition that does not have hydrogen to exist, the catalyst of load hydrogenation metal oxide is contacted with elementary sulfur, at least a portion of described elementary sulfur is entered in the hole of catalyst, contact with hydrogen-containing gas at 200 ℃～600 ℃ catalyst that will introduce sulphur.
US5139990 discloses a kind of Preparation of catalysts method that is used for the raw material of hydro carbons is carried out hydrotreatment, this method comprises that (1) obtains a kind of catalyst, this catalyst contains a kind of carrier material, and this carrier material deposits one or more raw materials to hydro carbons and carries out activated metal of hydrotreatment or metallic compound; (2) contact with the catalyst of step (1) with the liquid medium that contains organosulfur compound, introduce the organic sulfur compound of effective dose in the catalyst kind, described organosulfur compound is selected from following one group: the salt of ethylenebis (aminodithioformic acid), 2,5-dimercapto-1,3, the salt of 4-thiadiazoles, thiocarbamide, sulfo-hydracid ammonium, dimethyl sulfoxide (DMSO), 3,4-dithia adipate, 2,2-dithio glycol.
US5681787 discloses a kind of method for pre-sulphuration that contains the hydrogenation catalyst particle of at least a metal or metal oxide, this method comprises that (1) contacts described catalyst with elementary sulfur, the temperature of contact makes to small part sulphur and enters in the hole of catalyst, and (2) described catalyst is contacted with at least a oxygen-containing hydrocarbon class with at least 12 carbon atoms, obtain a kind of catalyst with self-heating character of reduction.
Through the hydrotreating catalyst of said method sulfuration, though its activity is improved, the phenomenon of the gathering of the active phase of sulphided state usually can appear in above-mentioned pre-vulcanization process, active sites quantity is reduced and the decentralization reduction.
CN 1256171A discloses the method for presulfurization outside a kind of on-the-spot device in the presence of hydrocarbon molecule, and the employed vulcanizing agent of this method is a hydrogen sulfide, hydrocarbon compound can be before catalyst vulcanization and/or during contact with catalyst.Hydrocarbon compound in this method is to be used for the hole of impregnated catalyst, can be oxycompound, also can be petroleum solvent.This method mainly is to carry out the gas phase presulfurization with hydrogen sulfide/hydrogen, and the concentration of hydrogen sulfide is not easy control, usually causes bed temperature runaway damage catalyst performance in sulfidation.In addition, the catalyst of this presulfurization preparation needs hydrocarbon compound is removed before unloading agent, and need carry out suitable oxidizing to a part of sulphided state catalyst and carry out Passivation Treatment, to guarantee safety in catalyst loading and unloading and transportation, the operating cost height that will cause presulfurization like this, and because catalyst repeatedly loads and unloads, cause a large amount of fragmentations of catalyst or intensity to reduce, very unfavorable to commercial Application.
Summary of the invention
For solving the deficiencies in the prior art, the invention provides a kind of method for pre-sulphuration of hydrogenation catalyst.When adopting the inventive method to carry out presulfurization, pre-curing temperature obviously reduces, and after presulfurization, the activity of hydrogenation catalyst is improved significantly.
Method provided by the invention is included under the presulfurization condition, in the presence of the gas of hydrogen, the sulfurized oil of a kind of Containing Sulfur agent and additive is contacted with the oxidation state hydrogenation catalyst carry out presulfurization.Wherein used additive is a polar organic compound, and its addition is the 0.01wt%～10wt% of sulfurized oil weight, is preferably 0.05wt%～5.0wt%, more preferably 0.1wt%～1.0wt%.
Described polar organic compound is the oxygen-containing hydrocarbon compounds, be selected from organic carboxyl acid, alcohols, ethers and the ester type compound one or more, be preferably alcohols, alcohols described here is one or more in isopropyl alcohol, n-butanol, isobutanol, propyl alcohol, glycerine, ethylene glycol and the diethylene glycol (DEG).
The gas of described hydrogen can be pure hydrogen, can be the gaseous mixture of hydrogen and inert gas also, is preferably pure hydrogen or the hydrogen content hydrogen of 80v% and the mist of inert gas at least, more preferably pure hydrogen.Here said pure hydrogen refers generally to the hydrogen of hydrogen purity greater than 98v%, and said inert gas generally is meant under the condition of described presulfurization, not with the gas of catalyst, feedstock oil and hydrogen generation chemical action.These gases include but not limited to the inert gas of zero group in nitrogen, the periodic table of elements etc., preferred nitrogen.
Described presulfurization is to adopt wet method presulfurization of the prior art, and used sulfurized oil of this process and vulcanizing agent have been conventionally known to one of skill in the art.Described sulfurized oil is selected from one or more of the various sulfurized oils that can be used for the wet method presulfurization, as in kerosene, light diesel fuel, atmosphere 3rd side cut distillate, decompression two wires distillate, reduce pressure three-way distillate, catalytic cracking diesel oil, the coker gas oil one or more, wherein preferred kerosene or light diesel fuel, more preferably kerosene.Described vulcanizing agent can be selected from one or more in the various vulcanizing agents that can be used for the wet method presulfurization, as carbon disulfide, mercaptan, thiophene and derivative thereof, dialkyl sulfide, as dimethylsulphide, dimethyl sulfide etc., preferred carbon disulfide or dimethyl sulfide, more preferably dimethyl sulfide.The content of vulcanizing agent in sulfurized oil is 0.1wt%～10wt%, is preferably 0.5wt%～5wt%, more preferably 1.0wt%～3.0wt%.Adopt conventional wet method method for pre-sulphuration, be preferably in before the presulfurization of hydrogenation catalyst wet method, feed sulfurized oil down earlier in lower temperature (normal temperature～150 ℃), wherein can add vulcanizing agent in the sulfurized oil, the control sulfur content is 0～2.0wt%, wetting beds, its operating condition is generally: air speed 0.1h
-1～10h
-1, time 0.1h～24h; Under the presulfurization condition, feed hydrogen then, and in sulfurized oil, add vulcanizing agent and polar organic compound.
Described presulfurization condition is as follows: temperature is 100 ℃～400 ℃, is preferably 150 ℃～350 ℃; Be 0.5h～24h time of contact, is preferably 4h～16h; The hydrogen dividing potential drop is 0.1MPa～15MPa, is preferably 1MPa～10MPa; Hydrogen to oil volume ratio is 50～2000, is preferably 100～1000; Volume space velocity is 0.2h during liquid
-1～5.0h
-1, be preferably 0.5h
-1～2.0h
-1
Described hydrogenation catalyst comprises Hydrobon catalyst, hydrotreating catalyst, hydrogenation protecting agent and hydrocracking catalyst, is preferably Hydrobon catalyst and hydrotreating catalyst.
Method for pre-sulphuration of the present invention can suppress the sulphided state activity and assemble mutually, can increase substantially the activity of hydrogenation catalyst.
The specific embodiment
Presulfurization oil and feedstock oil character used in the embodiment of the invention see Table 1.
The character of table 1 virgin kerosene and catalytic diesel oil
| The feedstock oil title | Virgin kerosene | Catalytic diesel oil |
| Density (20 ℃), g/cm 3 | 0.8044 | 0.8643 |
| Sulfur content, μ gg -1 | 460 | 6400 |
| Nitrogen content, μ gg -1 | 18 | 450 |
| Boiling range, ℃ (ASTMD86) | ||
| Initial boiling point | 148 | 171 |
| 10％ | 174 | 208 |
| 50％ | 188 | 259 |
| 90％ | 216 | 329 |
Give further instruction below by embodiment to technology of the present invention.
Comparative Examples 1
Method according to CN1288935A embodiment 3 prepares Hydrobon catalyst, catalyst be the cloverleaf pattern of diameter 1.2mm, it consists of 4.2wt%NiO, 18.5wt%WO
3, 8.9wt%MoO
3, 2.2wt%B
2O
3With the siliceous aluminium oxide of surplus (in the siliceous aluminium oxide, SiO
2Content is 14.1wt%).With length is that the strip catalyst of 3～8mm is packed in the fixed bed reactors, and feeding carbon disulfide content is the virgin kerosene (character sees Table 1) of 1.5wt%, is 320 ℃ in temperature, hydrogen dividing potential drop 6.0MPa, and liquid hourly space velocity (LHSV) is 1.0h
-1, hydrogen to oil volume ratio is under 300 the condition, to keep 12 hours, then, stops into sulfurized oil, switches catalytic diesel oil (character sees Table 1), is warmed up to 330 ℃, hydrogen dividing potential drop 6.0MPa, and liquid hourly space velocity (LHSV) is 2.0h
-1, hydrogen to oil volume ratio is 300.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Comparative Examples 2
Catalyst is with Comparative Examples 1, the method of CN1256171A embodiment 2 is adopted in presulfurization, be that catalyst is respectively 250 ℃ and 350 ℃ with initial boiling point and final boiling point at normal temperatures, density is the straight run hydrocarbon-fraction type diesel oil dipping of 0.837g/ml, the immersion amount is 39% of an oxide weight, is equivalent to 90% of available pore volume.Behind the dipping with solid in revolving burner, hydrogen in the stove and hydrogen sulfide sectional pressure are respectively 0.8 crust and 0.2 crust, temperature is 330 ℃, pass through presulfurization after, handle according to the activity rating of Comparative Examples 1, what obtain the results are shown in Table 2.
Embodiment 1
According to method pre-sulfide catalyst provided by the invention.
Except adding the diethylene glycol (DEG) of 0.5wt% in sulfurized oil, all the other are with Comparative Examples 1.Same feedstock oil is carried out hydrofinishing, reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 2
According to method pre-sulfide catalyst provided by the invention.
Except the n-butanol with 10wt% replaces the diethylene glycol (DEG) of 0.5wt%, all the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 3
According to method pre-sulfide catalyst provided by the invention.
Except the ethylene glycol with 1.0wt% replaces the diethylene glycol (DEG) of 0.5wt%, vulcanizing agent is a dimethyl sulfide.All the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 4
According to method pre-sulfide catalyst provided by the invention.
Remove the diethylene glycol (DEG) with the acetic acid substituted 0.5wt% of 0.01wt%, pre-curing temperature is outside 150 ℃, and all the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 5
According to method pre-sulfide catalyst provided by the invention.
Remove the diethylene glycol (DEG) that replaces 0.5wt% with the ethylene glycol of the ethyl acetate of 0.2wt% and 0.1wt%, pre-curing temperature is outside 200 ℃, and all the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 6
According to method pre-sulfide catalyst provided by the invention.
Remove the diethylene glycol (DEG) that replaces 0.5wt% with the divinyl ether of 0.6wt%, sulfurized oil is contacted with catalyst, air speed is 10h
-1, be 0.1h time of contact, begins then to heat up, and injects divinyl ether and vulcanizing agent carbon disulfide when temperature is raised to 100 ℃ in sulfurized oil, all the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 7
According to method pre-sulfide catalyst provided by the invention.
Except that at normal temperatures sulfurized oil is contacted with catalyst, air speed is 0.1h
-1, be 24h time of contact, begins then to heat up, and injects diethylene glycol (DEG) and vulcanizing agent carbon disulfide when temperature is raised to 380 ℃ in sulfurized oil, constant temperature sulfuration 4 hours, and all the other are with embodiment 1.Reaction running sampling after 100 hours, the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Embodiment 8
According to catalyst presulfurizing method provided by the invention.
Except used hydrogenation catalyst, pre-curing temperature with reaction temperature is different, all the other are with embodiment 1.The catalyst that present embodiment adopted is according to 14 preparations of embodiment among the CN1056514A, and it consists of 4.0wt%NiO, 17.5wt%WO
3, 0.5wt%F, surplus is the alumina support that contains 15wt%Y type zeolite.Pre-curing temperature is 230 ℃.Reaction temperature is 280 ℃, reaction running sampling after 100 hours, and the sulphur of analytic product oil, nitrogen content, and calculate desulfurization degree and denitrification percent, the results are shown in Table 2.
Table 2 result of the test
| The embodiment numbering | Denitrification percent, wt% | Desulfurization degree, wt% |
| Comparative Examples 1 | 78.6 | 94.1 |
| Comparative Examples 2 | 76.4 | 92.8 |
| Embodiment 1 | 84.3 | 96.9 |
| Embodiment 2 | 86.0 | 97.4 |
| Embodiment 3 | 82.5 | 95.3 |
| Embodiment 4 | 81.8 | 95.0 |
| Embodiment 5 | 83.3 | 97.9 |
| Embodiment 6 | 81.9 | 96.8 |
| Embodiment 7 | 82.0 | 98.1 |
| Embodiment 8 | 80.4 | 94.7 |
By the result of table 2 as can be seen, adopt method for pre-sulphuration provided by the invention to compare with conventional method (Comparative Examples 1), pre-curing temperature obviously reduces, and the HDS of catalyst and HDN activity are improved.Compare (Comparative Examples 2) with CN 1256171A disclosed method, use method presulfurization of the present invention after, the HDS of catalyst and HDN are active obviously to be improved.
Claims (7)
1, a kind of method for pre-sulphuration of hydrogenation catalyst, comprise join vulcanizing agent in the sulfurized oil after, under the presulfurization condition, in the presence of the gas of hydrogen, contact with the oxidation state hydrogenation catalyst and to carry out presulfurization, it is characterized in that adding polar organic compound in the described sulfurized oil, its addition is the 0.01wt%～10wt% of sulfurized oil weight; Described polar organic compound is one or more in n-butanol, isobutanol, propyl alcohol, glycerine, ethylene glycol, diethylene glycol (DEG), acetate, ethyl acetate and the divinyl ether.
2, method for pre-sulphuration according to claim 1 is characterized in that before presulfurization, earlier hydrogenation catalyst was contacted with sulfurized oil, and sulfur content is 0～2.0wt% in the sulfurized oil, and the operating condition of this process is: temperature is normal temperature～150 ℃, air speed 0.1h
-1～10h
-1, time 0.1h～24h.
3, method for pre-sulphuration according to claim 1, the addition that it is characterized in that described polar organic compound is the 0.05wt%～5.0wt% of sulfurized oil weight.
4, method for pre-sulphuration according to claim 1, the addition that it is characterized in that described polar organic compound is the 0.1wt%～1.0wt% of sulfurized oil weight.
5, method for pre-sulphuration according to claim 1, it is characterized in that described presulfurization is the wet method presulfurization, described sulfurized oil is one or more in kerosene, light diesel fuel, atmosphere 3rd side cut distillate, decompression two wires distillate, reduce pressure three-way distillate, catalytic cracking diesel oil and the coker gas oil; Described vulcanizing agent is one or more in carbon disulfide, mercaptan, thiophene and the dialkyl sulfide, and the content of vulcanizing agent in sulfurized oil is 0.1wt%～10wt%.
6, method for pre-sulphuration according to claim 1 is characterized in that described presulfurization condition is as follows: temperature is 50 ℃～400 ℃; Be 0.5h～24h time of contact; The hydrogen dividing potential drop is 0.1MPa～15MPa; Hydrogen to oil volume ratio is 50～2000; Volume space velocity is 0.2h during liquid
-1～5.0h
-1
7, method for pre-sulphuration according to claim 1 is characterized in that described hydrogenation catalyst comprises Hydrobon catalyst, hydrotreating catalyst, hydrogenation protecting agent and hydrocracking catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410050714XA CN100448542C (en) | 2004-10-29 | 2004-10-29 | Hydrogenation catalyst precuring method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410050714XA CN100448542C (en) | 2004-10-29 | 2004-10-29 | Hydrogenation catalyst precuring method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1769377A CN1769377A (en) | 2006-05-10 |
| CN100448542C true CN100448542C (en) | 2009-01-07 |
Family
ID=36750926
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200410050714XA Active CN100448542C (en) | 2004-10-29 | 2004-10-29 | Hydrogenation catalyst precuring method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100448542C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101260319B (en) * | 2008-04-25 | 2011-08-24 | 江苏佳誉信实业有限公司 | Vulcanization method for hydrogenation catalyst |
| CN106140314B (en) * | 2015-04-15 | 2018-07-31 | 中国石油化工股份有限公司 | A kind of hydrogenation catalyst and its application |
| CN106140313B (en) * | 2015-04-15 | 2018-09-28 | 中国石油化工股份有限公司 | A kind of hydrogenation catalyst and its application in hydrocarbon hydrogenation reaction |
| CN106140322B (en) * | 2015-04-15 | 2019-04-16 | 中国石油化工股份有限公司 | A kind of hydrogenation catalyst activation method and its application |
| CN106669860B (en) * | 2015-11-11 | 2019-03-19 | 中国石油化工股份有限公司 | A kind of vulcanization start-up method of Hydrobon catalyst |
| CN106179525A (en) * | 2016-07-22 | 2016-12-07 | 中国石油化工股份有限公司 | The method for pre-sulphuration of heavy-oil hydrogenation catalyst |
| CN110038582B (en) * | 2018-01-16 | 2022-03-08 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN114733578B (en) * | 2021-01-07 | 2024-01-05 | 中国石油化工股份有限公司 | Vulcanizing liquid and preparation method and application thereof |
| CN114958421A (en) * | 2021-02-23 | 2022-08-30 | 中国石油天然气股份有限公司 | Raw oil hydrogenation system, hydrogenation method and vulcanizing reagent |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1256171A (en) * | 1998-10-12 | 2000-06-14 | 欧洲催化剂加工公司 | Off-site presulphidation in the presence of hydrocarbon molecular |
| CN1270988A (en) * | 1999-04-20 | 2000-10-25 | 埃勒夫阿托化学有限公司 | Sulfurizing method for hydrogenation catalyst |
| US6218333B1 (en) * | 1999-02-15 | 2001-04-17 | Shell Oil Company | Preparation of a hydrotreating catalyst |
| CN1351111A (en) * | 2000-10-30 | 2002-05-29 | 中国石油化工股份有限公司 | Process for presulfurizing hydrocatalyst |
| WO2004091789A1 (en) * | 2003-04-07 | 2004-10-28 | Arkema | Method for treating hydroprocessing catalysts with an orthophthalate and sulphuration method using the same |
-
2004
- 2004-10-29 CN CNB200410050714XA patent/CN100448542C/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1256171A (en) * | 1998-10-12 | 2000-06-14 | 欧洲催化剂加工公司 | Off-site presulphidation in the presence of hydrocarbon molecular |
| US6218333B1 (en) * | 1999-02-15 | 2001-04-17 | Shell Oil Company | Preparation of a hydrotreating catalyst |
| CN1270988A (en) * | 1999-04-20 | 2000-10-25 | 埃勒夫阿托化学有限公司 | Sulfurizing method for hydrogenation catalyst |
| CN1351111A (en) * | 2000-10-30 | 2002-05-29 | 中国石油化工股份有限公司 | Process for presulfurizing hydrocatalyst |
| WO2004091789A1 (en) * | 2003-04-07 | 2004-10-28 | Arkema | Method for treating hydroprocessing catalysts with an orthophthalate and sulphuration method using the same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1769377A (en) | 2006-05-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2637345C (en) | Selective catalysts for naphtha hydrodesulfurization | |
| CA2912544C (en) | A hydroprocessing catalyst composition containing a heterocyclic polar compound, a method of making such a catalyst, and a process of using such catalyst | |
| CA2636156C (en) | Selective catalysts for naphtha hydrodesulfurization | |
| EP1994123B1 (en) | Selective catalysts having silica supports for naphtha hydrodesulfurization | |
| US9546327B2 (en) | Process for upgrading a high endpoint gas oil containing high concentrations of thiophenes and nitrogen and providing for a reduced hydrogen consumption rate | |
| JP4547922B2 (en) | Partially coked catalyst usable for hydrotreatment of fractions containing sulfur compounds and olefins | |
| CN101134909A (en) | Method of hydrodesulfuration of cuts containing sulphur compounds and olefins in the presence of a supported catalyst | |
| CA2695205A1 (en) | A composition useful in the catalytic hydroprocessing of hydrocarbon feedstocks, a method of making such catalyst, and a process of using such catalyst | |
| US9404053B2 (en) | Low-pressure process utilizing a stacked-bed system of specific catalysts for the hydrotreating of a gas oil feedstock | |
| CN105209579A (en) | Method for starting hydroprocessing or hydroconversion units | |
| CN100448542C (en) | Hydrogenation catalyst precuring method | |
| CA2840387C (en) | An ether amine additive impregnated composition useful in the catalytic hydroprocessing of hydrocarbons, a method of making such composition | |
| CN100448538C (en) | Distillate hydrogenation catalyst and its preparation method | |
| CN103386327A (en) | Selective hydrodesulfurization catalyst and preparation and application thereof | |
| US9724678B2 (en) | Process for preparing a sulphided catalyst | |
| RU2700685C2 (en) | Catalytic composition for hydrofining, containing acetoacetic acid compound, method of producing said catalyst and method of using said catalyst | |
| CN107456975B (en) | Hydrogenation catalyst, pretreatment method thereof, method for improving desulfurization activity of hydrogenation catalyst and application | |
| CN113908886A (en) | External presulfurization method of heavy oil hydrogenation catalyst and heavy oil hydrogenation presulfurization catalyst | |
| JPH08333582A (en) | Desulfurization of catalytically cracked gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |