CN109513456A - A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof - Google Patents
A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof Download PDFInfo
- Publication number
- CN109513456A CN109513456A CN201811428325.4A CN201811428325A CN109513456A CN 109513456 A CN109513456 A CN 109513456A CN 201811428325 A CN201811428325 A CN 201811428325A CN 109513456 A CN109513456 A CN 109513456A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- hours
- preparation
- constant temperature
- secondary hydrogenation
- 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
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J29/166—Y-type faujasite
-
- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
- C10G49/08—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
Landscapes
- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof, the composite oxides that catalyst of the invention is made of USY molecular sieve, aluminium oxide and nickel oxide are carrier, it calcines under high temperature environment, the active constituent of the catalyst is P, Mo, catalyst by weight percentage, each component content: P2O5Content is 4.0-6.0%, MoO3Content is 8.0-16.0%.Catalyst provided by the present invention is for cracking nine secondary hydrogenation of carbon, show high activity, high desulphurizing ability, with stronger anticol mass-energy power, it can adapt to the raw material of higher gum level, and catalyst service life is extended, which also effectively inhibits to overstock carbon, is improved catalyst stability.
Description
Technical field
The present invention relates to technical field of petrochemical industry, and in particular to a kind of nine secondary hydrogenation catalyst of cracking carbon and its preparation
Method.
Background technique
Crack carbon ninth is that cracking of ethylene by-product, mainly organize as C6-C12Hydrocarbons, account for ethylene yield
10%-20%.Due to containing the polymerizable active component and sulphur such as big weight phenylethylene, dicyclopentadiene, indenes, nitrogen in cracking carbon nine
Equal compounds, it is therefore necessary to remove the impurity such as unsaturates and sulphur, the nitrogen in carbon nine by hydrofinishing, can just be used for vapour
Oily blend component or aromatic solvent naphtha.Industrial cracking nine hydrofinishing of carbon at present is generally used two-stage hydrogenation technique, and one section
Adding hydrogen is mainly monoolefine by di-olefins, and alkenyl arene is converted into alkylaromatic hydrocarbon；Secondary hydrogenation is mainly by monoolefine
It is converted into saturated alkane, and removes the impurity such as sulphur, nitrogen.
Its light component C is concentrated mainly on to the research of nine secondary hydrogenation of carbon at present6-C8On drippolene, to nine full constituent of carbon
Add hydrogen research less, due to also containing C in carbon nine9-C12Heavy constituent, therefore colloid, the sulfur content in hydrogenating materials all can be a large amount of
Increase, the directly hydrogenation activity to secondary hydrogenation catalyst and anticol matter, more stringent requirements are proposed for anti-overstocked carbon ability.This hair
Bright to be intended to provide a kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof, the catalyst hydrogenation activity is high, anticol matter, anti-
It is strong to overstock carbon ability, extends the service life of catalyst.
Summary of the invention
According to above-mentioned elaboration, the present invention is intended to provide a kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof, is somebody's turn to do
Catalyst hydrogenation activity is high, and anticol matter, anti-overstocked carbon ability are strong, extends the service life of catalyst.
Technical solution provided by the invention:
A kind of nine secondary hydrogenation catalyst of cracking carbon, the catalyst are answered by what USY molecular sieve, aluminium oxide and nickel oxide were constituted
Oxide carrier is closed, by weight percentage: wherein the content of USY molecular sieve is 20%-40%, alumina content 1%-
3%, the content of nickel oxide is 40%-60%, and carrier is faintly acid, average pore size 15-25nm, specific surface area 140- after molding
220m2/ g, Kong Rong 0.5-1.5ml/g, the carrier have large aperture and specific surface faintly acid, greatly due to the addition of USY molecular sieve
The anticol mass-energy power and anti-overstocked carbon ability of catalyst are improved greatly.
The present invention also provides a kind of PMo catalyst prepared based on above-mentioned carrier, are used for nine secondary hydrogenation of carbon, show
Good reactivity, anticol matter and anti-overstocked carbon ability.Catalyst activity component content is calculated as with catalyst gross mass: P2O5
Content is 4.0-6.0%, MoO3Content is 8.0-16.0%.
The present invention provides the preparation method of above-mentioned catalyst, should the preparation method comprises the following steps:
Q1, by alumina powder, nickel oxide powder is mixed with USY powder, and a certain amount of boehmite, nitric acid and appropriate is added
Distilled water, stir evenly, roll rear extruded moulding, by environmental drying 6-12 hours of 100-150 DEG C, temperature is risen to
A kind of composite oxide carrier is made in 6 hours in 900 DEG C of calcinings；
Q2, the predecessor that the composite oxide carrier is impregnated to P and Mo are stood for 24 hours, small through 100-150 DEG C of dry 3-6
When, cracking nine secondary hydrogenation catalyst of carbon is made after temperature is risen to 800 DEG C of -1000 DEG C of calcinings 3-6 hours.
In above-mentioned technical proposal, in the Q1, the temperature rises to 900 DEG C of heating curve are as follows: 0-1 hour, is warming up to
It 300 DEG C, is kept for 1-2 hours under 300 DEG C of constant temperature；In 30 minutes, 600 DEG C are warming up to, 1-2 are kept under 600 DEG C of constant temperature
Hour；In 60 minutes, 400 DEG C are cooled to, is kept for half an hour under 400 DEG C of constant temperature；In 60 minutes, 900 DEG C are warming up to,
Calcining 6 hours is kept under 900 DEG C of constant temperature.
In above-mentioned technical proposal, in the Q2, the temperature rises to 800 DEG C-1000 DEG C of heating curve are as follows: 0-1 is small
When, 400 DEG C are warming up to, is kept for 1-1.5 hours under 400 DEG C of constant temperature；In 60 minutes, 600 DEG C are warming up to, in 600 DEG C of constant temperature
It is lower to be kept for 1-2 hours；In 40 minutes, 500 DEG C are cooled to, is kept for half an hour under 500 DEG C of constant temperature；In 90 minutes, rise
Temperature keeps calcining 3-6 hours to 800 DEG C -1000 DEG C under 800 DEG C of -1000 DEG C of constant temperature.
Compared to the prior art catalyst provided by the invention has the advantage that
(1), USY is the hydrocracking catalyst of widely used a kind of function admirable, and the present invention is added one in the carrier
Quantitative USY molecular sieve, and make it than being able to achieve the cracking of macromolecular colloid with moderate cracking ability by calcining, from
And the anticol mass-energy power of catalyst is substantially increased, the raw material of higher gum level can be adapted to, and extend catalyst
Service life；
(2), in carrier P and Mo addition, can inhibit the interaction of aluminium oxide and nickel oxide, reduce Surface acidity,
While keeping catalyst greater activity, also effectively inhibits to overstock carbon, be improved catalyst stability.
Specific embodiment
Technical solution of the present invention is clearly and completely described below, it is clear that described embodiment is only this
Invention a part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art exist
Every other embodiment obtained under the premise of creative work is not made, shall fall within the protection scope of the present invention.
Embodiment 1
By USY molecular sieve 20.0g, alumina powder 1.0g, boehmite 100g, the nitric acid 10g of 2% concentration is added,
100g distilled water, stirs evenly after rolling, and squeezes as bar shaped, through 100 DEG C environmental drying 6 hours, by temperature in 0-1 hours time
300 DEG C are risen in section, calcining at constant temperature 60 minutes, then in 30 minutes, are warming up to 600 DEG C, constant temperature is kept for 60 minutes, then will be warm
Degree is cooled to 400 DEG C in 60 minutes, and constant temperature is kept for 30 minutes, and finally temperature rises to 900 DEG C in 60 minutes, calcining at constant temperature
A kind of composite oxide carrier, specific surface area 140m is made within 6 hours2The carrier is named as A carrier by/g, Kong Rong 0.5ml/g.
Embodiment 2
By USY molecular sieve 30g, alumina powder 2.0g, boehmite 150g, the nitric acid 20g, 200g of 2% concentration is added
Distilled water stirs evenly after rolling, and squeezes as bar shaped, through 120 DEG C environmental drying 8 hours, by temperature in 0-1 hour period
It rises to 300 DEG C, calcining at constant temperature 120 minutes, then in 30 minutes, is warming up to 600 DEG C, constant temperature is kept for 120 minutes, then by temperature
400 DEG C are cooled in 60 minutes, constant temperature is kept for 30 minutes, and finally temperature rises to 900 DEG C in 60 minutes, calcining at constant temperature 6
A kind of composite oxide carrier, specific surface area 140m is made in hour2The carrier is named as B carrier by/g, Kong Rong 0.5ml/g.
Embodiment 3
Phosphorus pentoxide 8g, ammonium heptamolybdate salt 16g are weighed, PMo maceration extract is configured to suitable quantity of water dissolution, then using leaching
The maceration extract is carried on 90gA carrier by stain method, 3 hours dry through 100 DEG C by standing for 24 hours, in 0-1 hour period
It is interior, 400 DEG C are warming up to, is kept for 1 hour under 400 DEG C of constant temperature, in 60 minutes, temperature is risen to 600 DEG C, in 600 DEG C of constant temperature
It is lower to be kept for 1 hour, then in 40 minutes, 500 DEG C are cooled to, is kept for half an hour under 500 DEG C of constant temperature；Finally at 90 minutes
It is interior, 800 DEG C are warming up to, cracking nine secondary hydrogenation catalyst A1 of carbon is made after keeping under 800 DEG C of constant temperature calcining 3 hours.
Embodiment 4
Phosphorus pentoxide 14g, ammonium heptamolybdate salt 22g are weighed, PMo maceration extract is configured to suitable quantity of water dissolution, then uses
The maceration extract was carried on 120gB carrier by infusion process, 3 hours dry through 100 DEG C by standing for 24 hours, in 0-1 hour time
In section, 400 DEG C are warming up to, is kept for 1.5 hours under 400 DEG C of constant temperature, in 60 minutes, temperature is risen to 600 DEG C, at 600 DEG C
It is kept for 2 hours under constant temperature, then in 40 minutes, is cooled to 500 DEG C, is kept for half an hour under 500 DEG C of constant temperature；Finally 90
In minute, 1000 DEG C are warming up to, cracking nine secondary hydrogenation catalyst of carbon is made after keeping under 1000 DEG C of constant temperature calcining 6 hours
B1。
Comparative example 1
Nickel nitrate hexahydrate 8g, ammonium heptamolybdate salt 16g are weighed, NiMo maceration extract is configured to suitable quantity of water dissolution, then adopts
The maceration extract is carried on 90gA carrier with infusion process, it is 3 hours dry through 100 DEG C by standing for 24 hours, at 0-1 hour
Between in section, be warming up to 400 DEG C, kept for 1 hour under 400 DEG C of constant temperature, in 60 minutes, temperature is risen to 600 DEG C, at 600 DEG C
It is kept for 1 hour under constant temperature, then in 40 minutes, is cooled to 500 DEG C, is kept for half an hour under 500 DEG C of constant temperature；Finally 90
In minute, 800 DEG C are warming up to, cracking nine secondary hydrogenation catalyst C1 of carbon is made after keeping under 800 DEG C of constant temperature calcining 3 hours.
Comparative example 2
Nickel nitrate hexahydrate 14g, ammonium heptamolybdate salt 22g are weighed, NiMo maceration extract is configured to suitable quantity of water dissolution, then adopts
The maceration extract is carried on 120gB carrier with infusion process, it is 3 hours dry through 100 DEG C by standing for 24 hours, at 0-1 hour
Between in section, be warming up to 400 DEG C, kept for 1.5 hours under 400 DEG C of constant temperature, in 60 minutes, temperature is risen to 600 DEG C, 600
It is kept for 2 hours under DEG C constant temperature, then in 40 minutes, is cooled to 500 DEG C, is kept for half an hour under 500 DEG C of constant temperature；Finally exist
In 90 minutes, 1000 DEG C are warming up to, cracking nine secondary hydrogenation catalyst of carbon is made after keeping under 1000 DEG C of constant temperature calcining 6 hours
C2。
Embodiment 5
Using embodiment catalyst A1, B1, C1, C2 respectively to C6-C9Hydrogenation products are that raw material carries out selection plus hydrogen, reaction
Evaluation carries out on 100ml isothermal bed hydroprocessing reaction unit, and catalyst is first in 3.0Mpa, 350 DEG C, oil product air speed 2.0h-1, comment
Valence 100 hours, every 10 hours sampling analyses were evaluated the Hydrogenation of A1, B1, C1, C2 catalyst, result such as table
Shown in 1.
Using heating curve stage by stage, it is therefore intended that in entire temperature-rise period, composite oxide carrier composition is brilliant
Body can more merge intact.
Table 1
As it can be seen from table 1 A1, B1 catalyst all have fine desulfurization, deolefination activity, gum level is also at a fairly low,
The USY molecular sieve of high activity is added in catalyst, so that catalyst has the cracking performance of height to macromolecular colloid, P component is deposited
, catalyst greater activity is not only maintained, also restrained effectively overstocked carbon, so that catalyst stabilization performance improves, it is right
Ratio C1, C2 selects tradition NiMo maceration extract to make catalyst, and desulfurization contains, deolefination activity is lower, and gum level is higher, C1,
Although C2 catalyst also contains USY molecular sieve, carrier increases passivity in calcination process after impregnating, reduces molecular sieve
Activity, catalytic performance are not so good as PMo maceration extract.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (8)
1. a kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof, it is characterised in that: the catalyst carrier is with USY
The composite oxides that molecular sieve, aluminium oxide and nickel oxide are constituted are carrier, are calcined under high temperature environment, the work of the catalyst
Property component be P, Mo；
Preparation method is as follows:
Q1, by alumina powder, nickel oxide powder is mixed with USY powder, and a certain amount of boehmite, nitric acid and suitable steaming is added
Distilled water stirs evenly, and rolls rear extruded moulding, and by environmental drying 6-12 hours of 100-150 DEG C, temperature is risen to 900 DEG C
A kind of composite oxide carrier is made in 6 hours in calcining；
Q2, the predecessor that the composite oxide carrier is impregnated to P and Mo are stood for 24 hours, 3-6 hours dry through 100-150 DEG C, will
Cracking nine secondary hydrogenation catalyst of carbon is made in temperature after rising to 800 DEG C of -1000 DEG C of calcinings 3-6 hours.
2. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: institute
Composite oxide carrier is stated, by weight percentage, each group is divided into the content 20%-40% of USY molecular sieve, alumina content
1%-3%, the content 40%-60% of nickel oxide.
3. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: institute
Catalyst is stated, by weight percentage, each group is divided into P2O5Content is 4.0-6.0%, MoO3Content is 8.0-16.0%.
4. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: should
Composite oxide carrier average pore size is 15-25nm, specific surface area 140-220m2/ g, Kong Rong 0.5-1.5ml/g.
5. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: add
The concentration of nitric acid entered is 2%, is calculated with the gross mass of catalyst, and nitric acid quality accounting is 1-3%.
6. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: add
The predecessor for entering P is phosphorus pentoxide, and the predecessor of Mo is ammonium heptamolybdate.
7. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 1 and preparation method thereof, it is characterised in that: institute
It states in Q1, the temperature rises to 900 DEG C of heating curve are as follows: 0-1 hour, be warming up to 300 DEG C, kept under 300 DEG C of constant temperature
1-2 hours；In 30 minutes, 600 DEG C are warming up to, is kept for 1-2 hours under 600 DEG C of constant temperature；In 60 minutes, it is cooled to
400 DEG C, kept for half an hour under 400 DEG C of constant temperature；In 60 minutes, 900 DEG C are warming up to, calcining 6 is kept under 900 DEG C of constant temperature
Hour.
8. a kind of nine secondary hydrogenation catalyst of cracking carbon according to claim 7 and preparation method thereof, it is characterised in that: institute
It states in Q2, the temperature rises to 800 DEG C-1000 DEG C of heating curve are as follows: 0-1 hour, 400 DEG C are warming up to, in 400 DEG C of constant temperature
It is lower to be kept for 1-1.5 hours；In 60 minutes, 600 DEG C are warming up to, is kept for 1-2 hours under 600 DEG C of constant temperature；In 40 minutes,
500 DEG C are cooled to, is kept for half an hour under 500 DEG C of constant temperature；In 90 minutes, be warming up to 800 DEG C -1000 DEG C, 800 DEG C -
Calcining 6 hours is kept under 1000 DEG C of constant temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811428325.4A CN109513456A (en) | 2018-11-27 | 2018-11-27 | A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811428325.4A CN109513456A (en) | 2018-11-27 | 2018-11-27 | A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109513456A true CN109513456A (en) | 2019-03-26 |
Family
ID=65794370
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811428325.4A Pending CN109513456A (en) | 2018-11-27 | 2018-11-27 | A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109513456A (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2258476A1 (en) * | 2008-03-28 | 2010-12-08 | Petroleum Energy Center, A Juridical Incorporated Foundation | Hydrocracking catalyst for heavy oil |
| CN103611562A (en) * | 2013-11-29 | 2014-03-05 | 武汉科林精细化工有限公司 | Catalyst for pyrolysis C9 two-stage hydrogenation and preparation method thereof |
-
2018
- 2018-11-27 CN CN201811428325.4A patent/CN109513456A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2258476A1 (en) * | 2008-03-28 | 2010-12-08 | Petroleum Energy Center, A Juridical Incorporated Foundation | Hydrocracking catalyst for heavy oil |
| CN103611562A (en) * | 2013-11-29 | 2014-03-05 | 武汉科林精细化工有限公司 | Catalyst for pyrolysis C9 two-stage hydrogenation and preparation method thereof |
Non-Patent Citations (3)
| Title |
|---|
| 张莎: "Ni-Mo型润滑油加氢处理催化剂研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
| 曹光伟: "加氢处理催化剂的制备和表征 Ⅰ. MoNiP/Al2O3催化剂的制备及助剂的作用", 《催化学报》 * |
| 陈绍洲等: "《石油加工工艺学》", 31 December 1997, 华东理工大学出版社 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4762814A (en) | Hydrotreating catalyst and process for its preparation | |
| CN107812525B (en) | A kind of method of hydrogenating catalyst composition and hydrotreating | |
| CN105126815B (en) | A kind of inferior heavy oil suspension bed hydrogenation catalyst and its preparation and application | |
| CN100590180C (en) | Diesel oil fraction upgrading and pour point reducing process | |
| US4707246A (en) | Hydrotreating catalyst and process | |
| CN101905165B (en) | Preparation and application of catalyst for selective hydrodesulfurization of gasoline | |
| CN106607096B (en) | A kind of hydrogenation catalyst and preparation method thereof | |
| CN105521791B (en) | The preparation method of vulcanization type catalyst for selective hydrodesulfurizationof of gasoline | |
| CN101376110A (en) | Preparation of hydrogenation catalyst | |
| CN102451722A (en) | Preparation method of eggshell-type hydrogenation catalyst | |
| CN101108363A (en) | Manufacturing method of catalyzer used for low quality light oil catalytic reforming and application thereof | |
| CN102051204B (en) | Work starting method for hydrogenation process | |
| CN102500403A (en) | Liquefied gas hydrogenating, olefin content decreasing and desulfurizing catalyst and preparation method thereof | |
| CN102989493A (en) | Heavy oil hydrotreating composite catalyst preparation method | |
| CN109395770A (en) | A kind of iron-based hydrogenation catalyst and preparation method thereof | |
| CN106552640B (en) | Reformer feed catalyst for pre-hydrogenation and preparation method thereof | |
| CN106607097B (en) | A kind of hydrogenation catalyst and preparation method thereof | |
| CN105582963B (en) | A kind of preparation method of vulcanization type catalyst for selective hydrodesulfurizationof of gasoline | |
| CN100413587C (en) | Sulfurized type catalyst, and its prepn. method | |
| CN105233848A (en) | Ni, W and P loaded hydrofining catalyst with three-peak type pore size distribution for anthracene oil, and preparation method and application | |
| CN100478423C (en) | Selective hydrogenation desulfuration catalyst for catalytically cracking gasoline and its preparation method | |
| CN100360231C (en) | Hydrogenating catalyst composition and preparation process thereof | |
| CN109513456A (en) | A kind of nine secondary hydrogenation catalyst of cracking carbon and preparation method thereof | |
| CN108421554A (en) | Hydrobon catalyst and its preparation method and application | |
| CN101280220B (en) | Method for producing good quality ethylene material by hydrogenation and dearomatization of benzin naphtha |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190326 |
|
| RJ01 | Rejection of invention patent application after publication |