CN1861260A - Sulfurized hydrogenation catalyst, prepn. method - Google Patents
Sulfurized hydrogenation catalyst, prepn. method Download PDFInfo
- Publication number
- CN1861260A CN1861260A CN 200510046431 CN200510046431A CN1861260A CN 1861260 A CN1861260 A CN 1861260A CN 200510046431 CN200510046431 CN 200510046431 CN 200510046431 A CN200510046431 A CN 200510046431A CN 1861260 A CN1861260 A CN 1861260A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- accordance
- elementary sulfur
- organic solvent
- sulfur
- 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.)
- Granted
Links
Abstract
A process for preparing the sulfurizing hydrocatalyst used for the hydrodesulfurizing and hydrodenitrifying reactions of light fractional oil and the hydrosaturating of arylhydrocarbon includes such steps as carrying a certain part of the precursor compound of the metal in VI and VIII families, introducing sulfur to it, heat treating, introducing the rest of said precursor compound, and drying.
Description
Technical field
The present invention relates to a kind of preparation method of high activity catalyst for hydrogenating hydrocarbon oil, with the oily needs of producing of the light ends that satisfies cleaning.
Background technology
Hydrogenation catalyst is used to handle that hydrocarbon ils carries out hydrodesulfurization, hydrodenitrogeneration under the condition that hydrogen exists, hydrogenation is saturated and reaction such as hydrocracking, hydrogenation catalyst is a carrier with the stronger inorganic oxide of adsorption capacity such as aluminium oxide, titanium oxide, silica and aluminium oxide and silica compound, VI family comprises metals such as Mo and/or W in the load periodic table of elements on carrier, metals such as Co of VIII family and/or Ni, these metals exist with oxide form.The oxide form catalyst activity is lower, changes into corresponding metal sulfide usually and just has higher activity, therefore must carry out presulfurization and handle after catalyst is packed hydrogenation plant into.When the reactive metal high degree of dispersion of sulphided state, catalyst just has high activity.
The method for pre-sulphuration of prior art, mainly comprise methods such as outer presulfurization of device and the interior presulfurization of device, these methods all are to add vulcanizing agent after Preparation of Catalyst is finished or the oxidation state reactive metal is converted into sulphided state, carry out certain processing then, preserve, transport and use with suitable.These methods are carried out the presulfurization of Preparation of Catalyst and catalyst respectively, both are not combined, and the serviceability of catalyst can also further be improved.As USP5017535, EP 329499, CN1107539C etc. promptly be Preparation of Catalyst is finished after, again sulphur-containing substance is loaded on the catalyst.
Start with in order to make catalyst obtain serviceability preferably, to have in the prior art from the Preparation of catalysts method.For example Japanese patent application publication No. 59-102442 and 59-69147 have mentioned a series of methods that prepare catalyst, according to said method, and with the reactive metal aqueous solution oxide impregnation alumina supporter that contains the carboxylic-acid substance, roasting then.Carboxylic acids thing such as citric acid, malic acid etc. form complex with reactive metal.To contain amino, cyano group organic compound in the European patent 0181035, as follows amion acetic acid, disodium salt or diethylenetriamines etc. add the aqueous solution of reactive metals, and the catalyst of making is dry under less than 200 ℃ temperature.Make activity of such catalysts metal dispersity height like this, activity of such catalysts can improve.Above-mentioned catalyst preparation process has just been added some auxiliary agents in the reactive metal dipping solution, improve the serviceability of catalyst to a certain extent, but directly Preparation of catalysts process and pre-vulcanization process is not combined.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of hydrogenization catalyst preparation method, the inventive method can obtain a kind of hydrogenation catalyst that contains vulcanizing agent, and preparation process is simple, and catalyst vulcanization is abundant, and is active high.
Hydrogenation catalyst preparation process of the present invention may further comprise the steps:
(1) get or prepare the catalyst intermediate that contains the partial hydrogenation reactive metal oxides, reactive metal oxides is 2%～85% of a final catalyst requirement, and is preferred 5%～70%, most preferably 25%～70%;
(2) catalyst intermediate that obtains in the step (1) is introduced elementary sulfur (being elemental sulfur);
(3) material that obtains of step (2) is heat-treated;
(4) the hydrogenation active metals component of dipping surplus is also dry, is finally contained the hydrogenation catalyst of vulcanizing agent.
Wherein the described hydrogenation active metals of step (1) generally is selected from one or more among W, Mo, Ni, the Co, and content can need to determine, generally count 1%～50% of catalyst weight with oxide by using.
When the described catalyst intermediate of step (2) is introduced elementary sulfur, introduce organic solvent before and in the step of one afterwards or a few step.The concrete grammar of introducing organic solvent and elementary sulfur (elemental sulfur) can adopt one of various possible modes in the prior art, loads to earlier on the catalyst as (1) elementary sulfur, floods organic solvent then; (2) elementary sulfur is dispersed in the organic solvent, is incorporated on the catalyst jointly then; (3) earlier organic solvent is impregnated on the catalyst, introduces elementary sulfur then; (4) earlier organic solvent is impregnated on the catalyst, mixes with the elementary sulfur pressed powder then.The elementary sulfur consumption is generally the total theoretical metal of catalyst and needs 30%～120%, preferred 80%～105% of sulfur content.Catalyst is theoretical need sulfur content to be that institute's metallic components is converted into sulfide (Co on the catalyst
9S
8, MoS
2, Ni
3S
2, WS
2) time need the amount of sulphur.The organic solution consumption can be generally 0.05%～50% of catalyst intermediate weight by this area general condition operation, and is preferred 1%～50%, and more preferably 2%～30%.Organic solvent can adopt operable all kinds of solvents in the Containing Sulfur agent catalyst preparation process, and those skilled in the art know these solvents.In some organic solvents commonly used such as hydrocarbon ils, oxygen-bearing organic matter, sulfurous organic compound, the itrogenous organic substance etc. one or more.Oxygen-bearing organic matter is preferably selected organic carboxylic ester, and itrogenous organic substance is preferably selected organic amine or organic amino compounds, and sulfurous organic compound is preferably selected organic polysulfide.Oxygen-bearing organic matter, itrogenous organic substance etc. also can be introduced before elementary sulfur is introduced catalyst intermediate, and consumption is 0.1～7 with total metal molar ratio.Hydrocarbon ils generally can be from the heavy end wet goods of various naphthas, gasoline, kerosene, diesel oil, white oil, lam-oil, lube base oil, straight run and decompression one or more, the hydrocarbon ils that obtains of secondary operations preferably, the above-mentioned hydrocarbon ils that obtains as technologies such as catalytic cracking, thermal cracking.Organic carboxylic ester can be the organic carboxylic ester that contains 6～60 carbon atoms, the preferred fat acid glyceride.As sesame oil, safflower seed oil, corn oil, cottonseed oil, peanut oil, rapeseed oil, soya-bean oil, walnut oil, coconut oil, olive oil, sunflower oil, lard, n-butyl acetate, 1-Methoxy-2-propyl acetate, 1, the 4-butanediol diacrylate, the cyclohexylenedinitrilotetraacetic acid isopropyl ester, hexa-methylene-1,6 vulcabond, triethyl phosphate, methyl phenylacetate, isobutyl phenylacetate, the terephthalic acid (TPA) dinonyl, repefral, diethyl phthalate, Methyl Salicylate, butyl p-hydroxybenzoate, and in similar other organic carboxylic ester etc. one or more.Hydrocarbon ils, organic carboxylic ester can be used alone, but also also mix together, and use its weight ratio can be 1: 10～10: 1 (hydrocarbon ils: organic carboxylic ester) if mix.Can add an amount of sulfurous organic compound in the organic solvent, as sulfone class material, thio-alcohol material, thiurams material, organic polysulfide etc. one or more.
The described heat treatment process of step (3) is to handle 1～40 hour down at 100～300 ℃, and heat treated can be an inert gas environment, also can be that oxygen content is the oxygen atmosphere that has of 0.1v%～30v%.Heat treated pressure can be that normal pressure is to 3MPa.
The described dipping residual metallic of step (4) method can adopt conventional dipping process, descends dry 1～30 hour at 80～200 ℃ then, obtains final catalyst prod.
(1) and/or (4) step process in can add the required auxiliary agent of catalyst, as phosphorus, boron, silicon, fluorine, titanium, zirconium etc., the auxiliary agent use amount can be as required determined by this area general knowledge.
Find after deliberation, in the Preparation of catalysts process, support certain component active metal component earlier, introduce elementary sulfur then, the component of load residual metallic again, the catalyst that obtains like this has good presulfurization effect, has good serviceability during application.The present invention mainly provides the method for preparing high activated catalyst, can satisfy the needs of the light ends oil production of cleaning, the present invention has solved the complicated and inadequate problem of sulfuration of the sulfidation that exists in early stage technology and the method for preparing catalyst through repeatedly experimental study.Introduce behind the vulcanizing agent through certain heat treatment, and follow-up dipping active metal component and dry the processing, these introduce the processing procedure behind the vulcanizing agent, make catalyst thermal discharge when using activation of Containing Sulfur agent few, and heat release is even in the activation process, has controlled concentrated heat release problem effectively.
The specific embodiment
Further specify the process of the inventive method below by specific embodiment, wherein Chang Gui technology contents can be determined according to general knowledge and needs by those skilled in the art, does not therefore limit the scope of the invention.
Embodiment 1
Hydrogenation catalyst A: with the gama-alumina is carrier, and reactive metal consists of: Mo content is with MoO
3The meter weight percentage is 23.7%, and Co content is 4.5% in the CoO weight percentage, and P content is with P
2O
5The meter weight percentage is 3.1%.(disregarding the composition of vulcanizing agent)
Contain the above-mentioned composition Preparation of catalysts of vulcanizing agent process:
Get 1000 gram gamma-aluminium oxide carriers, the carrier specific area is 296m
2/ g, pore volume 0.87ml/g, with 129 gram molybdenum trioxides, 56 gram cobalt carbonates, 30.6 gram 85% phosphoric acid and an amount of water are mixed with the 900ml aqueous solution, flood above-mentioned carrier, and dipping sample later makes catalyst intermediate 340 ℃ of dryings 4 hours, and Mo content is with MoO
3The meter weight percentage is 10%, and Co content is 2% in the CoO weight percentage, and P content is with P
2O
5The meter weight percentage is 1.5%.The mixed solvent of 91.2 gram lactic acid and 5 gram triethanolamines is incorporated on the above-mentioned catalyst intermediate of 250 grams, introduces the elementary sulfur powder then, and handled 10 hours at 150 ℃ of normal pressures.The elementary sulfur consumption is 105% of a final catalyst activity theoretical metal need sulfur content.With 117 gram molybdenum trioxides, 67 gram cobalt carbonates, 25.7 gram 85% phosphoric acid and an amount of water are mixed with the semi-finished product of 780ml solution impregnating catalyst at last, and 120 ℃ dry 5 hours down, make finished catalyst (numbering catalyst A).The feedstock oil of catalyst A activity rating is Kuwait's normal pressure diesel oil, is the main character about feedstock oil below.
Embodiment 2
Hydrogenation catalyst A: with the gama-alumina is carrier, and reactive metal consists of: Mo content is with MoO
3The meter weight percentage is 25.8%, and Co content is 4.9% in the CoO weight percentage, and P content is with P
2O
5The meter weight percentage is 3.5%.(disregarding the composition of vulcanizing agent)
Contain the above-mentioned composition Preparation of catalysts of vulcanizing agent process:
Get 1000 gram gamma-aluminium oxide carriers, the carrier specific area is 296m
2/ g, pore volume 0.87ml/g, with 129 gram molybdenum trioxides, 56 gram cobalt carbonates, 30.6 gram 85% phosphoric acid and an amount of water are mixed with the 1300ml aqueous solution, flood above-mentioned carrier, and dipping sample later makes catalyst intermediate 340 ℃ of dryings 4 hours, and Mo content is with MoO
3The meter weight percentage is 8.9%, and Co content is 1.7% in the CoO weight percentage, and P content is with P
2O
5The meter weight percentage is 1.1%.It is in 1: 5 the solvent that the elementary sulfur powder is dispersed in catalytic cracking diesel oil and rapeseed oil volume ratio, solvent load is 15% of a catalyst intermediate weight, the elementary sulfur consumption is theoretical 37% of the sulfur content that needs of final catalyst metals, handled 5 hours at 180 ℃ in obturator then, final pressure is 0.4MPa (gauge pressure).With 120 gram molybdenum trioxides, 70 gram cobalt carbonates, 26.5 gram 85% phosphoric acid and an amount of water are mixed with the semi-finished product of 650ml solution impregnating catalyst at last, and 110 ℃ dry 6 hours down, make finished catalyst (numbering catalyst B).The feedstock oil of catalyst B activity rating is Kuwait's normal pressure diesel oil, is the main character about feedstock oil below.
Embodiment 3
According to the method for embodiment 1, active metallic content is 15% (weight) of final catalyst activity tenor in the minimizing catalyst intermediate, and the elementary sulfur use amount is 80% of a theoretical requirement, and other presses embodiment 1 method, gets catalyst C.
Embodiment 4
Press the method for embodiment 2, active metallic content is 70% (weight) of final catalyst activity tenor in the increase catalyst intermediate, and the elementary sulfur use amount is 110% of a theoretical requirement, and other presses the method for embodiment 2, gets catalyst D.
Embodiment 5
Hydrogenation catalyst E, carrier γ-Al
2O
3, active metal W O
319.3wt%, MoO
36.7wt%, NiO 4.2wt%.(disregarding the composition of vulcanizing agent)
Get the carrier identical, earlier with the whole MoO of infusion process load with embodiment 2
3And NiO, to press the method for embodiment 2 then and introduce elementary sulfur and solvent, the consumption of elementary sulfur is theoretical 98% of sulfur content, the final impregnating method load WO of needing of final catalyst
3, get catalyst E.
Comparative example 1
Get the oxidized catalyst with embodiment 1 same composition, press method and the condition of introducing elementary sulfur among the embodiment 1, introduces identical sulphur and solvent (being that catalyst is introduced elementary sulfur at last), must catalyst F.
The character of table 1 Kuwait normal pressure diesel oil
| Proportion | 0.8504 |
| Sulfur content (wt%) | 1.623 |
| Nitrogen content (μ g/g) | 730 |
| Boiling range, (℃) | |
| Initial boiling point | 234 |
| 50% (v) distillates a little | 316 |
| The end point of distillation | 389 |
The process conditions of table 2 evaluation test
| Reaction pressure (MPa) | 3.0 |
| Liquid hourly space velocity (LHSV) (h -1) | 2 |
| Reaction temperature (℃) | 330 |
| Hydrogen to oil volume ratio (v) | 350 |
| The duration of runs (hr) | 100 |
The activity of catalyst sample is represented (is 100 with comparative example) with relative hydrodesulfurization rate with relative hydrodenitrogeneration rate, the results are shown in Table 3.
Table 3 embodiment and comparative example evaluating catalyst performance
| Catalyst | A | B | C | D | E | F |
| Relative desulfurization degree | 135 | 128 | 114 | 108 | 127 | 100 |
| Relative denitrification percent | 129 | 125 | 112 | 106 | 148 | 100 |
| Maximum bed temperature rise in the activation process, ℃ | 15 | 16 | 18 | 19 | 17 | 26 |
Claims (12)
1, a kind of preparation method of sulfurized hydrogenation catalyst may further comprise the steps:
(1) get or prepare the catalyst intermediate that contains the partial hydrogenation reactive metal oxides, reactive metal oxides is 2%～85% of a final catalyst requirement;
(2) catalyst intermediate that obtains in the step (1) is introduced elementary sulfur;
(3) material that obtains of step (2) is heat-treated;
(4) the hydrogenation active metals component of dipping surplus is also dry, is finally contained the hydrogenation catalyst of vulcanizing agent.
2, in accordance with the method for claim 1, it is characterized in that reactive metal oxides is 5%～70% of a final catalyst requirement in the described catalyst intermediate.
3, in accordance with the method for claim 1, it is characterized in that reactive metal oxides is 25%～70% of a final catalyst requirement in the described catalyst intermediate.
4, in accordance with the method for claim 1, it is characterized in that described hydrogenation active metals is selected from one or more among W, Mo, Ni, the Co.
When 5, in accordance with the method for claim 1, it is characterized in that the described catalyst intermediate of step (2) is introduced elementary sulfur, introduce organic solvent before and in the step of one afterwards or a few step.
6, in accordance with the method for claim 5, it is characterized in that the method for described catalyst intermediate introducing organic solvent of step (2) and elementary sulfur can adopt one of following manner, (1) elementary sulfur loads to earlier on the catalyst, floods organic solvent then; (2) elementary sulfur is dispersed in the organic solvent, is incorporated on the catalyst jointly then; (3) earlier organic solvent is impregnated on the catalyst, introduces elementary sulfur then; (4) earlier organic solvent is impregnated on the catalyst, mixes with the elementary sulfur pressed powder then.
7, in accordance with the method for claim 1, it is characterized in that the described elementary sulfur consumption of step (2) is that the total theoretical metal of catalyst needs 30%～120% of sulfur content.
8, in accordance with the method for claim 1, it is characterized in that the described elementary sulfur consumption of step (2) is that the total theoretical metal of catalyst needs 80%～105% of sulfur content.
9, in accordance with the method for claim 1, it is characterized in that the described heat treatment process of step (3) is for handling 1～40 hour down at 100～300 ℃.
10, in accordance with the method for claim 9, it is characterized in that described heat treated is an inert gas environment, or oxygen content is the oxygen atmosphere that has of 0.1v%～30v%, heat treated pressure is that normal pressure is to 3MPa.
11, in accordance with the method for claim 1, it is characterized in that the described dipping residual metallic of step (4) method adopts conventional dipping process, descended dry 1～30 hour at 80～200 ℃ then, obtain final catalyst prod.
12,, it is characterized in that the described consumption of organic solvent of step (2) is 0.05%～50% of a catalyst intermediate weight according to claim 5 or 6 described methods.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100464312A CN100360237C (en) | 2005-05-12 | 2005-05-12 | Sulfurized hydrogenation catalyst, prepn. method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100464312A CN100360237C (en) | 2005-05-12 | 2005-05-12 | Sulfurized hydrogenation catalyst, prepn. method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1861260A true CN1861260A (en) | 2006-11-15 |
| CN100360237C CN100360237C (en) | 2008-01-09 |
Family
ID=37388843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100464312A Active CN100360237C (en) | 2005-05-12 | 2005-05-12 | Sulfurized hydrogenation catalyst, prepn. method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100360237C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100453180C (en) * | 2006-12-20 | 2009-01-21 | 中国科学院山西煤炭化学研究所 | Hydrogenation catalyst precuring method |
| CN101890381B (en) * | 2009-05-19 | 2012-07-18 | 中国石油化工股份有限公司 | Hydrotreating guard catalyst and application thereof |
| CN102039147B (en) * | 2009-10-21 | 2012-08-29 | 中国石油化工股份有限公司 | Preparation method of vulcanized catalyst |
| CN101890383B (en) * | 2009-05-19 | 2012-08-29 | 中国石油化工股份有限公司 | Hydrodenitrogenation catalyst and application thereof |
| CN103801334A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Preparation method of sulfuration-type hydrogenation catalyst |
| CN111744517A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744516A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744515A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5139990A (en) * | 1988-07-29 | 1992-08-18 | Akzo Nv | Process for the preparation of a resulfided catalyst |
| FR2689420B1 (en) * | 1992-04-01 | 1994-06-17 | Eurecat Europ Retrait Catalys | PROCESS FOR PRESULFURIZING A HYDROCARBON PROCESSING CATALYST. |
| FR2758478B1 (en) * | 1997-01-21 | 1999-02-26 | Elf Aquitaine | PROCESS FOR THE PRESULFURIZATION OF CATALYSTS |
| CN1268433C (en) * | 2003-10-31 | 2006-08-09 | 中国石油化工股份有限公司 | Prevulcanizing method for hydrogenating catalyst |
-
2005
- 2005-05-12 CN CNB2005100464312A patent/CN100360237C/en active Active
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100453180C (en) * | 2006-12-20 | 2009-01-21 | 中国科学院山西煤炭化学研究所 | Hydrogenation catalyst precuring method |
| CN101890381B (en) * | 2009-05-19 | 2012-07-18 | 中国石油化工股份有限公司 | Hydrotreating guard catalyst and application thereof |
| CN101890383B (en) * | 2009-05-19 | 2012-08-29 | 中国石油化工股份有限公司 | Hydrodenitrogenation catalyst and application thereof |
| CN102039147B (en) * | 2009-10-21 | 2012-08-29 | 中国石油化工股份有限公司 | Preparation method of vulcanized catalyst |
| CN103801334A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Preparation method of sulfuration-type hydrogenation catalyst |
| CN103801334B (en) * | 2012-11-08 | 2016-01-06 | 中国石油化工股份有限公司 | A kind of preparation method of sulfurized hydrogenation catalyst |
| CN111744517A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744516A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744515A (en) * | 2019-03-29 | 2020-10-09 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744515B (en) * | 2019-03-29 | 2022-10-21 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744517B (en) * | 2019-03-29 | 2022-10-21 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
| CN111744516B (en) * | 2019-03-29 | 2022-11-15 | 中国石油化工股份有限公司 | Hydrotreating catalyst and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100360237C (en) | 2008-01-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100360237C (en) | Sulfurized hydrogenation catalyst, prepn. method | |
| JP3855090B2 (en) | Off-site pretreatment method for hydrocarbon treatment catalysts | |
| CN100360236C (en) | Treatment method before application of hydrogenation catalyst | |
| EP2173477B1 (en) | Method for the production of a catalyst for hydrocarbon hydrotreatment. | |
| KR101311968B1 (en) | Hydrogenation catalyst composition, process for preparing the same and use thereof | |
| JPH0639299A (en) | Method for preliminary sulfurization of hydrocarbon treating catalyst | |
| CN100525915C (en) | preparation process of vulcanized hydrogenation catalyst | |
| JP3676849B2 (en) | Gas oil hydrodesulfurization catalyst | |
| CN101417230B (en) | Processing method before applying hydrogenation catalyst | |
| CN101417245B (en) | Hydrogenation catalyst processing method | |
| CN107456974A (en) | A kind of hydrogenation catalyst and its preprocess method methods and applications desulphurizing activated with hydrogenation catalyst is improved | |
| CN100525912C (en) | Treatment method before application of hydrogenation catalyst | |
| CN107457006A (en) | A kind of hydrogenation catalyst and its preprocess method methods and applications desulphurizing activated with hydrogenation catalyst is improved | |
| CN100413587C (en) | Sulfurized type catalyst, and its prepn. method | |
| CN101148607B (en) | Hydrocarbon hydroprocessing technique | |
| CN100360231C (en) | Hydrogenating catalyst composition and preparation process thereof | |
| CN101148608B (en) | Hydrocarbon hydroprocessing technique | |
| CN1611577A (en) | Prevulcanizing method for hydrogenating catalyst | |
| CN100413588C (en) | Hydrogenation catalyst composition and its prepn. method | |
| CN1356377A (en) | Catalyst for selectively hydrodesulfurizing gasoline and its preparing process | |
| CN101417246A (en) | Processing method before using hydrogenation catalyst | |
| JP3339588B2 (en) | Method for producing catalyst for hydrotreating hydrocarbon oil | |
| CN109926102B (en) | Hydrogenation catalyst composition and preparation method thereof | |
| CN114733577B (en) | Sulfuration type hydrogenation catalyst, preparation method and application thereof | |
| CN103769243B (en) | The ex situ presulfiding method of hydrogenation catalyst |
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 |