CN102019201A - Molecular sieve-containing heavy distillate hydrorefining catalyst - Google Patents
Molecular sieve-containing heavy distillate hydrorefining catalyst Download PDFInfo
- Publication number
- CN102019201A CN102019201A CN2009100920915A CN200910092091A CN102019201A CN 102019201 A CN102019201 A CN 102019201A CN 2009100920915 A CN2009100920915 A CN 2009100920915A CN 200910092091 A CN200910092091 A CN 200910092091A CN 102019201 A CN102019201 A CN 102019201A
- Authority
- CN
- China
- Prior art keywords
- molecular sieve
- catalyst
- heavy distillate
- oil
- carrier
- 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.)
- Pending
Links
Landscapes
- Catalysts (AREA)
Abstract
The invention relates to a molecular sieve-containing heavy distillate hydrorefining catalyst. Aluminum oxide, an aluminophosphate molecular sieve and a titanium silicalite molecular sieve are taken as carriers; at least one of Fe, Co, Ni metals and at least one of Mo and W metals are taken as active ingredients; and the molecular sieve-containing heavy distillate hydrorefining catalyst comprises the following components in percentage by weight: 1 to 40 percent of aluminophosphate molecular sieves, 1 to 40 percent of titanium silicalite molecular sieves, 20 to 80 percent of aluminum oxide, 1 to 10 percent of one or more of Fe, Co and Ni and 5 to 40 percent of one or more of Mo and W. The catalyst is used for performing hydrodesulfurization and hydrodenitrogeneration on basic oil for lubricating oil, and heavy distillates at the temperature of more than 350 DEG C; when the basic oil for the lubricating oil is processed, the sulfur content of the prepared oil is reduced to below 2mu g/g and the nitrogen content is reduced to 20mu g/g; and when inferior Shengli vacuum gas oil (VGO) and Canada oil-sand bitumen are processed, the sulfur content of the prepared oil can be reduced to below 10mu g/g and the nitrogen content is reduced to below 200mu g/g.
Description
Technical field
The present invention relates to a kind of heavy distillate Hydrobon catalyst that contains molecular sieve, be specially adapted to the hydrodesulfurization and the hydrodenitrogeneration of inferior heavy oil cut in the petroleum refining field.
Background technology
In petroleum refining industry, along with the aggravation of crude oil heaviness, inferiorization trend, cause impurity content height such as sulphur in the heavy distillate, nitrogen, heavy distillate is carried out deep hydrofinishing, can significantly reduce the content of impurity such as its sulphur, nitrogen, thereby reduce environmental pollution.
Hydrobon catalyst is a carrier with composite oxides such as aluminium oxide or aluminium oxide and silica, boron oxide, zirconias generally, with group vib W, Mo is the active component element, with the Co of VIII family, Ni is the adjuvant component element, their various combination, its catalytic performance respectively has characteristics, and for example Co-Mo combination has stronger desulphurizing activated; Ni-Mo combination and Ni-W combination have stronger denitrogenation and arene saturating activity.In order further to improve the performance of catalyst, also add other and add component, as P, F, B, Ti, Zr etc.
CN1765509A discloses a kind of macropore alumina supporter, with the aluminium oxide is main component, contain boron oxide, it is characterized in that the weight content of boron oxide in carrier is 1 ω %～15 ω %, average pore size 10nm～20nm, carrier 〉=350 ℃ meleic acid is 0.05mmol/g～0.3mmol/g, and the pore volume of carrier is 0.5cm
3/ g～1.0cm
3/ g, specific area is 150m
2/ g～270m
2/ g.The temperature of boron is introduced in this patent control in alumina precursor, adopt this method when obtaining macropore alumina supporter, and the acid amount in the carrier increases.But the increase of acid amount can cause the bad stability of catalyst.
CN101332430A discloses a kind of heavy oil hydrogenating treatment catalyst and preparation method thereof, and this catalyst contains carrier and at least a VIII of being selected from family and at least a metal component that is selected from group vib, and wherein carrier is a kind of composite alumina support of boracic.This catalyst hydrogenation is handled active higher, and stability better.
US5089453 adopts kneading method to prepare residual oil hydrocatalyst, adopts to add acid solution earlier in its preparation process, adds the alkaline solution neutralization again, uses a large amount of TiCl simultaneously
4Make improvements agent, it is higher to contain the Ti amount in the catalyst, because TiCl
4Hydrolysis produces harmful fog, makes will use specialized apparatus in the production process, generates the technology more complicated, and the production difficulty is big, and security is low.
US6387248 adopts dried kneading method to prepare residual oil hydrocatalyst, and with phosphorus as auxiliary agent.Metal is that the form with metal salt powder joins in the alumina powder, cause the active metal component skewness easily, and the intensity of catalyst is also relatively poor relatively.
Summary of the invention
The purpose of this invention is to provide the Hydrobon catalyst that a kind of preparation technology is simple, with low cost, can significantly reduce heavy distillate sulphur, nitrogen content under the condition that relaxes, be specially adapted to lube base oil in the petroleum refining field and greater than the hydrodesulfurization and the hydrodenitrogeneration of 350 ℃ of heavy distillates.
Heavy distillate Hydrobon catalyst of the present invention comprises following component: aluminium oxide, phosphate aluminium molecular sieve AlPO
4, titanium silicon molecular sieve ETS-4 and reactive metal.Wherein preferably a kind of code name of phosphate aluminium molecular sieve is AlPO
4-5 phosphate aluminium molecular sieve, phosphate aluminium molecular sieve can be to carry out cation exchange with ammonium salt, or Titanium, silicon, nickel, molybdenum or zirconium metallic salt carry out modification, and wherein modified metal is 0～5% of a total catalyst weight; The HTS that preferably a kind of code name of HTS is ETS-10, HTS can be to carry out cation exchange with ammonium salt, or metallic iron, zinc, lanthanum, nickel, molybdenum or aluminum metal salt carry out modification, and wherein modified metal is 0～5% of a total catalyst weight; Active metal component is at least a Fe, Co, Ni and at least a Mo, W.
Each components contents is as follows in the heavy distillate Hydrobon catalyst of the present invention: with the weight percent meter of catalyst, the content of phosphate aluminium molecular sieve is 1～40%, preferably 5～30%; The content of HTS is 1～40%, preferably 5～30%; The content of aluminium oxide is 20～80%, preferably 30～60%; Among active metal component Fe, Co, the Ni one or more, content are 1～10%, preferably 3～8%; Among active metal component Mo, the W one or more, content are 5～40%, preferably 10～30%.
Hydrobon catalyst of the present invention is with aluminium oxide, phosphate aluminium molecular sieve AlPO
4, titanium silicon molecular sieve ETS-4 is carrier, wherein aluminium oxide is the main carrier component of catalyst, Heat stability is good, pore-size distribution are suitable; Two kinds of different molecular sieves are handled by suitable modification as the main acidic components of catalyst, and are acid adjustable, and can increase the specific area of carrier.
The specific area of catalyst for hydrorefining distillate oil of the present invention is 150m
2/ g～300m
2/ g, pore volume are 0.30cm
3/ g～0.70cm
3/ g, average pore size is 8nm～20nm, wherein the pore size distribution of aperture 〉=10nm accounts for 60%～90% of total pore volume.
Carried metal of the present invention adopts the soluble salt aqueous solution of respective metal, loads on the catalyst by the mode of flooding.
Preparation of catalysts method of the present invention comprises, with molecular sieve dry powder, aluminium oxide, binding agent and extrusion aid, mixes by a certain percentage, and extruded moulding, drying, roasting obtain catalyst carrier.With the salting liquid of described metallic compound step impregnation or soak altogether sequentially, pass through health, drying, roasting then again, obtain catalyst.
Catalyst of the present invention adopts phosphate aluminium molecular sieve AlPO
4-5 and titanium silicon molecular sieve ETS-4-10, by the synergy of two kinds of molecular sieves, improve the hydrofinishing performance of catalyst, make its processing heavy distillate inferior under the process conditions that relax, reach the effect of deep desulfuration, denitrogenation.
Compared with prior art, catalyst of the present invention adopts phosphate aluminium molecular sieve AlPO simultaneously
4-5 and titanium silicon molecular sieve ETS-4-10, by the synergy of two kinds of molecular sieves, improve the hydrofinishing performance of catalyst, make its processing heavy distillate inferior under the process conditions that relax, reach the effect of deep desulfuration, denitrogenation.
The specific embodiment
A kind of heavy distillate Hydrobon catalyst employed titanium silicon molecular sieve ETS-4-10 character that contains molecular sieve of the present invention is as follows: TiO
2/ SiO
2Mol ratio is 0.1～0.5, preferably 0.15～0.45, and Na
2O weight content＜0.2 ω %, best＜0.15 ω %.
A kind of employed phosphate aluminium molecular sieve AlPO of heavy distillate Hydrobon catalyst that contains molecular sieve of the present invention
4-5 character are as follows: P
2O
5/ Al
2O
3Mol ratio is 1.0～5.0, preferably 1.5～4.5, and Fe
2O
3Weight content＜0.5 ω %, best＜0.4 ω %, Na
2O weight content＜0.2 ω %, best＜0.15 ω %.
Aluminium oxide used in the present invention is commercially available boehmite, or has the commercial alumina carrier of suitable pore size distribution.
Catalyst of the present invention can use the adhesive component of refractory inorganic oxides as catalyst when preparing carriers, as in clay, silica, aluminium oxide, sial, zirconia, the titanium oxide one or more, binder wt is 0～40% of a final catalyst.Also can not add adhesive component when catalyst carrier of the present invention prepares, but directly add Ludox, mix the moulding of pinching bar.
The present invention is in the Preparation of catalysts process, can adopt extrusion aid during extrusion, extrusion aid commonly used can be one or more in sesbania powder, citric acid, tartaric acid, oxalic acid, cellulose, starch, the high molecular surfactant, preferably sesbania powder and citric acid.
The shape of catalyst of the present invention can be sheet, sphere, cylinder bar or special-shaped bar (clover, bunge bedstraw herb), preferably cylinder bar and special-shaped bar (clover, bunge bedstraw herb).The diameter of catalyst can be 0.8mm～2.0mm slice or＞the thick bar of 2.5mm, the preferably slice of 1.0mm～1.8mm.
Catalyst of the present invention can be at 350 ℃～380 ℃ of reaction temperatures, hydrogen dividing potential drop 8.0MPa～14.0MPa, volume space velocity 0.5h
-1～2.0h
-1Hydrogen to oil volume ratio 500～800: under 1 the process conditions, the raw material of lubricating oil for machining base oil 650SN, the sulfur content that generates oil is reduced to below the 2 μ g/g, nitrogen content is reduced to below the 20 μ g/g, processing triumph inferior VGO and Canadian oil sands bitumen, the sulfur content that generates oil can be reduced to below the 10 μ g/g, and nitrogen content is reduced to below the 200 μ g/g.
The following examples will give further instruction to a kind of heavy distillate Hydrobon catalyst that contains molecular sieve provided by the invention, but not thereby limiting the invention.
Embodiment 1
Get the boehmite that 200g Shanxi Aluminum Co., Ltd produces, add 10g sesbania powder, mix, the mixed solution that dropping is made up of 10g nitric acid, 10g citric acid and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 120 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst A.
Embodiment 2
Get boehmite, 35g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,25g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 120 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst B.
Embodiment 3
Get boehmite, 35g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,25g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid, 20g Ludox and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Be mixed with to such an extent that maceration extract floods with ammonium fluoride, 120 ℃ of dry 4h, 350 ℃ of roasting 4h, the maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 120 ℃ of dry 4h, 550 ℃ of roasting 4h make catalyst C.
Embodiment 4
Get boehmite, 35g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,25g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid, 20g Ludox and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 120 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst D.
Embodiment 5
Get boehmite, 35g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,25g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate, ammonium molybdate and SPA preparation floods again, 120 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst E.
Embodiment 6
Get boehmite, 25g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,15g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 120 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst F.
Embodiment 7
Get boehmite, 25g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,15g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and drip the mixed solution of being made up of 15g nitric acid, 10g citric acid, 20g Ludox and 200g deionized water, mixed pinching, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate preparation floods again, 110 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst G.
Embodiment 8
Get boehmite, 25g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,15g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and drip the mixed solution of being made up of 15g nitric acid, 10g citric acid and 200g deionized water, mix pinch, cloverleaf pattern that extrusion becomes 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate, basic cobaltous carbonate and ammonium molybdate and SPA preparation floods again, 110 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst H.
Embodiment 9
Get boehmite, 35g phosphate aluminium molecular sieve AlPO that 200g Shanxi Aluminum Co., Ltd produces
4-5,25g titanium silicon molecular sieve ETS-4-10 and 10g sesbania powder mix, and the mixed solution that dropping is made up of 15g nitric acid, 10g citric acid and 200g deionized water mixes to be pinched, extrusion becomes the cloverleaf pattern of 1.5mm, 110 ℃ of dry 2h at 550 ℃ of roasting 4h, make carrier then.Maceration extract with nickel nitrate and ammonium molybdate and SPA preparation floods again, 110 ℃ of dry 4h, and 550 ℃ of roasting 4h make catalyst I.
Comparative example 1
A kind of industrial heavy distillate hydrofinishing agent J, hydrogenation active metals is cobalt, molybdenum, nickel, fluorine.This catalyst is carrier with the aluminium oxide, with ammonium fluoride dipping, and 110 ℃ of dry 4h, 320 ℃ of shallow degree roasting 4h, again with the co-impregnated solution dipping of nickel nitrate and ammonium molybdate and basic cobaltous carbonate preparation, 110 ℃ of dry 4h, 550 ℃ of roasting 4h and making.
Table 1 catalyst is formed
Embodiment 10
The micro anti-evaluation result of the above-mentioned catalyst of this case introduction.
The catalytic amount that micro anti-evaluation uses is 1.5g, serve as to estimate raw material in n-decane solution that contains dibenzothiophenes (in sulphur 1000 μ g/g) and the n-decane solution that contains pyridine (with nitrogen 500 μ g/g) respectively, carry out hydrodesulfurization and hydrodenitrogeneration performance comparison test, reaction condition sees Table 2.
The little anti-hydrogenation appreciation condition of table 2
The micro anti-evaluation of catalyst the results are shown in Table 3.
The little anti-hydrogenation evaluation result of table 3
As can be seen from Table 3, the hydrodesulfurization, the hydrodenitrogenationactivity activity that add the catalyst B of molecular sieve are greatly increased than catalyst A, after suitable introducing auxiliary agents of silicon, phosphorus, the hydrodesulfurization of catalyst D, E, G, hydrodenitrogeneration performance are got back and are further improved, and the introducing of auxiliary agent fluorine slightly reduces the hydrodesulfurization performance of catalyst C.Use cobalt, molybdenum, nickel to be higher than and use molybdenum, nickel catalyst I as reactive metal as hydrodesulfurization, the hydrodenitrogeneration performance of the catalyst of reactive metal.Find that simultaneously when active metal component was identical, the hydrogenation activity of the catalyst of introducing molecular sieve 30 ω % was apparently higher than the catalyst of introducing molecular sieve 20 ω %.As seen, the hydrogenation performance of the Hydrobon catalyst of introducing molecular sieve is better than adopting the industrial hydrogenation catalyst J of traditional handicraft preparation.
Embodiment 11
Present embodiment adopts 100ml hydrogenation evaluating apparatus, and VGO is a raw material with triumph, and catalyst D, J are carried out single hop list agent hydrogenation performance evaluation, and reaction condition sees Table 4.
Table 4100ml hydrogenation appreciation condition
The 100ml evaluation result of catalyst sees Table 5.
Table 5 catalyst contrast hydrogenation evaluation result
Embodiment 12
Present embodiment adopts 100ml hydrogenation evaluating apparatus, is raw material with sulphur, the higher lube base oil 650SN of nitrogen content, and catalyst D, J are carried out single hop list agent hydrogenation performance evaluation, and reaction condition sees Table 6.
Table 6100ml hydrogenation appreciation condition
The 100ml evaluation result of catalyst sees Table 7.
Table 7 catalyst contrast hydrogenation evaluation result
By table 5 and table 7 as seen, compare with the industrial hydrogenation catalyst J that adopts the traditional handicraft preparation, hydrodesulfurization, the nitrogen removal performance of Hydrobon catalyst D of introducing molecular sieve is good, can be applicable to the hydrotreatment of heavy distillate.
Embodiment 13
Present embodiment adopts 100ml hydrogenation evaluating apparatus, and big with density, sulphur, the higher Canadian oil sands bitumen of nitrogen content are raw material, and catalyst D, J are carried out single hop list agent hydrogenation performance evaluation, and reaction condition sees Table 8.
Table 8100ml hydrogenation appreciation condition
The 100ml evaluation result of catalyst sees Table 9.
Table 9 catalyst contrast hydrogenation evaluation result
By table 9 as seen, the Hydrobon catalyst D that introduces molecular sieve has possessed raw material adaptive capacity preferably, and the inferior heavy oil that density is big, the sulphur nitrogen content is high is also had good hydrogenation effect, is a kind of effective heavy distillate Hydrobon catalyst.
Claims (7)
1. heavy distillate Hydrobon catalyst that contains molecular sieve, it is characterized in that: this catalyst is to be carrier with aluminium oxide, phosphate aluminium molecular sieve and HTS, with at least a Fe, Co, Ni metal and at least a Mo, W metal is active component, by total catalyst weight 100%: phosphate aluminium molecular sieve is 1～40%, HTS is 1～40%, aluminium oxide is 20～80%, among Fe, Co, the Ni one or more are 1～10%, and one or more among Mo, the W are 5～40%.
2. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 1 is characterized in that: phosphate aluminium molecular sieve and HTS are the phosphate aluminium molecular sieve AlPO of modification in the carrier
4-5 and titanium silicon molecular sieve ETS-4-10.
3. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 1, it is characterized in that: aluminium oxide is a boehmite in the carrier.
4. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 1, it is characterized in that: phosphate aluminium molecular sieve is to carry out cation exchange with ammonium salt, or Titanium, silicon, nickel, molybdenum or zirconium metallic salt carry out modification, and wherein modified metal is 0～5% of a total catalyst weight.
5. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 1, it is characterized in that: HTS is to carry out cation exchange with ammonium salt, or metallic iron, zinc, lanthanum, nickel, molybdenum or aluminum metal salt carry out modification, and wherein modified metal is 0～5% of a total catalyst weight.
6. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 1 is characterized in that: the profile of catalyst is bar shaped, cloverleaf pattern, graininess or tooth sphere.
7. a kind of heavy distillate Hydrobon catalyst that contains molecular sieve according to claim 2 is characterized in that: this catalyst is used for lube base oil and greater than the hydrodesulfurization and the hydrodenitrogeneration of 350 ℃ heavy distillate after sulfuration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100920915A CN102019201A (en) | 2009-09-15 | 2009-09-15 | Molecular sieve-containing heavy distillate hydrorefining catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100920915A CN102019201A (en) | 2009-09-15 | 2009-09-15 | Molecular sieve-containing heavy distillate hydrorefining catalyst |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102019201A true CN102019201A (en) | 2011-04-20 |
Family
ID=43861225
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009100920915A Pending CN102019201A (en) | 2009-09-15 | 2009-09-15 | Molecular sieve-containing heavy distillate hydrorefining catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102019201A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103100402A (en) * | 2011-11-09 | 2013-05-15 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN105728059A (en) * | 2014-12-10 | 2016-07-06 | 中国石油天然气股份有限公司 | Catalyst carrier, preparation method therefor and application of catalyst carrier |
| CN108452844A (en) * | 2017-10-27 | 2018-08-28 | 中国石油天然气股份有限公司 | A kind of diesel oil hydrofining catalyst and its preparation method and application |
| CN110180580A (en) * | 2019-05-21 | 2019-08-30 | 北京高新利华科技股份有限公司 | Gasoline hydrogenation treatment catalyst and preparation method thereof |
-
2009
- 2009-09-15 CN CN2009100920915A patent/CN102019201A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103100402A (en) * | 2011-11-09 | 2013-05-15 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN103100402B (en) * | 2011-11-09 | 2015-06-17 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN105728059A (en) * | 2014-12-10 | 2016-07-06 | 中国石油天然气股份有限公司 | Catalyst carrier, preparation method therefor and application of catalyst carrier |
| CN108452844A (en) * | 2017-10-27 | 2018-08-28 | 中国石油天然气股份有限公司 | A kind of diesel oil hydrofining catalyst and its preparation method and application |
| CN110180580A (en) * | 2019-05-21 | 2019-08-30 | 北京高新利华科技股份有限公司 | Gasoline hydrogenation treatment catalyst and preparation method thereof |
| CN110180580B (en) * | 2019-05-21 | 2022-09-30 | 北京高新利华科技股份有限公司 | Gasoline hydrofining catalyst and preparation method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102151582B (en) | Preparation method of hydrodesulfurization catalyst for high-nitrogen low-quality gasoline and diesel | |
| CN100548479C (en) | A kind of titania-alumina mixed oxide Hydrobon catalyst and preparation method | |
| CN102247864A (en) | Preparation method of catalyst for hydrogenation desulfurization and denitrification of light-weight oil | |
| CN101590424B (en) | Hydrogenation catalyst of distillate oil and preparation method thereof | |
| CN103551162A (en) | Diesel hydrodesulfurization and denitrification catalyst and preparation method thereof | |
| CN102051206B (en) | Method for producing ethylene cracking materials by hydrofining naphtha | |
| JP5922372B2 (en) | Hydrotreating catalyst and method for producing the same | |
| CN102876365B (en) | Method for grading catalysts for hydrofining of inferior distillate oil | |
| WO2013095856A1 (en) | Silica containing alumina supports, catalysts made therefrom and processes using the same | |
| CN103769179B (en) | A kind of preparation method of catalyst for hydrotreatment of residual oil | |
| CN102019201A (en) | Molecular sieve-containing heavy distillate hydrorefining catalyst | |
| CN101905175B (en) | Method for preparing heavy distillate hydrotreating catalyst | |
| CN103372457A (en) | Catalytic cracking diesel oil hydro-upgrading catalyst and application thereof | |
| CN108786869B (en) | Diesel oil deep hydrogenation catalyst, preparation method and application thereof | |
| CN101204659B (en) | Hydrogenation catalyst using Al, Ti and Si compound oxide as carrier and preparation method thereof | |
| CN103861647B (en) | A kind of hydrocracking catalyst containing heteropoly acid and application thereof | |
| CN102851061B (en) | Hydrofining method of low-grade gasoline/diesel oil | |
| CN102806088A (en) | Preparation method of reformer feed hydrogenation pre-refining catalyst | |
| CN100478423C (en) | Selective hydrogenation desulfuration catalyst for catalytically cracking gasoline and its preparation method | |
| CN102284300A (en) | Catalyst for poor diesel hydrotreatment and preparation method | |
| CN106179388B (en) | A kind of preparation method of hydrotreating catalyst | |
| CN109794299A (en) | A kind of hydrogenation catalyst and preparation method thereof, fraction oil hydrogenation refining method | |
| KR20000053177A (en) | Catalyst containing phosphorus and method for hydro-treating oil feedstocks with this catalyst | |
| CN106311254B (en) | A kind of residual oil hydrocatalyst and preparation method and method of hydrotreating | |
| CN104923244B (en) | Diesel oil hydrofining catalyst and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20110420 |