CN1179462A - Process for preparing heavy oil cracking catalyst - Google Patents
Process for preparing heavy oil cracking catalyst Download PDFInfo
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- CN1179462A CN1179462A CN 97108204 CN97108204A CN1179462A CN 1179462 A CN1179462 A CN 1179462A CN 97108204 CN97108204 CN 97108204 CN 97108204 A CN97108204 A CN 97108204A CN 1179462 A CN1179462 A CN 1179462A
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- heavy oil
- preparation
- ore deposit
- oil cracking
- catalyst
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
A fixed-bed or fluidized-bed catalyst for cracking heavy oil is prepred from cheaper loess ore and features high poisoning resistance, low reaction temp, high output rate and quality of products, saving energy and no pollution.
Description
The present invention relates to a kind of Preparation of catalysts method, especially a kind of in petrochemical industry, be used for the preparation method of heavy oil cracking catalysts.
Current, China's petrochemical system mainly adopts molecular sieve catalyst to the cracking and the cracking of oil (containing heavy oil), and this catalyzer has following weakness:
1, catalyzer is easily poisoned, and contains S, N and heavy metal Fe, Cu, Ni, V, particularly Ni in the heavy oil, and V and alkali N poison catalyzer, so heavy oil is wanted removal of impurities in advance.
2, can not carry out catalytic cracking and cracking to 100% heavy oil, heavy oil can only mix 50%, and all the other use lighter wax oil etc.
3, in heavy oil catalytic pyrolysis reaction, must be in raw material hydrogen make-up, add water vapor or hydrogen.
4, molecular sieve catalyst is made complexity, the price height, and per ton more than 1.5 ten thousand yuan, what have must be from external import, and price is higher, and the foreign exchange spending is big.
5, reaction is not thorough, is exactly some cut of catalytic cracking underpressure distillation and remaining residual oil or slurry oil as pressure fuel.
The preparation method who the purpose of this invention is to provide a kind of heavy oil cracking catalyst, by the catalyzer of this method preparation, the anti-poisoning improved the utilization ratio of oil, step-down refining of petroleum and tooling cost, the quality of raising refining of petroleum product.
Technical scheme of the present invention is such: a kind of preparation method of heavy oil cracking catalyst: the loess ore deposit is dried or dried, pulverize, sieve with 100 mesh sieve, remove impurity, Powdered loess ore deposit, water is heated to boiling after, add binding agent, stir fully that the dissolving back adds Powdered loess ore deposit, look after fully stirring evenly plasticity-and quantitatively; Extrusion molding is dried under 200-300 ℃ of condition, is contained in the high-temperature resistant container, at 600-700 ℃ of following secluding air, keeps sintering 2 hours; Stop heating, slowly cooling is taken out, and gets the fixed bed catalyst finished product.
The loess ore deposit is dried or dried, be ground into the powdery granule of diameter 40 μ m with pulverizer; After water is heated to boiling, add A-S glue, stir, fully after the dissolving, add Powdered loess ore deposit, be made into flowable viscous fluid, sending spraying to be shaped then, microspherical catalyst.
The fixed bed catalyst finished product is beaten broken, porphyrize sieves with 200 mesh sieve, and undersized powder or powder sieve with 350 mesh sieve again, get the powder on the sieve, the fluid catalyst finished product.
Binding agent is polyvinyl alcohol or A-S glue.
The container of anti-the climax is a stainless steel tube.
The present invention has following advantage:
1, the preparation method is simple, and raw material is obtained easily, thereby the catalyzer of preparation is cheap.
2, the catalyzer toxin immunity by this method preparation is strong, and heavy oil does not need to do any S of removing, and removing heavy metals removes pre-treatment such as alkali N, and the fusing that directly heats up is with regard to catalyzed reaction, and repeated regeneration, life-time service.
3, carry out the reaction that the cracking of heavy oil is split with the catalyzer of this method preparation, temperature of reaction is low, and temperature is at 460 °--and between 490 ℃, therefore, required equipment is simple, and cost is low, save energy.
Embodiment one: fixed bed catalyst
The loess ore deposit is dried or dried, machinery or artificial the pulverizing, with the shakeout removal of impurities of sieving of 100 mesh sieve, must powder stock.Heat water to boiling, add polyvinyl alcohol, after stirring makes dissolving fully, add Powdered loess ore deposit, make Powdered loess ore deposit form the plasticity-solid, pass through squeezer then, being squeezed into diameter is the round stripe shape of 3mm, under 200-300 ℃ of condition, dry, reinstall in stainless steel vessel, put the interior temperature control of electric tube furnace at 600-720 ℃ of secluding air, calcined 2 hours, stop heating, slowly cooling is taken out.
Embodiment two: fluid catalyst:
With the said fixing bed catalyst, to beat brokenly, porphyrize sieves with 200 mesh sieve, and undersized powder or powder sieve with 350 mesh sieves again, get the powder above the sieve, and the powder diameter can be directly used in fluidized-bed between the 80-40 micron.
Embodiment three: microspheric catalyst:
The loess ore deposit is dried or dried, after the pulverizing, produce the powder shaped loess ore deposit of diameter people 40 μ m with the column mill porphyrize, after water is heated to boiling, after adding the abundant dissolving of A.S glue (by the aqueous solution of preparations such as activated alumina) stirring, be added in Powdered loess ore deposit, be made into flowable viscous fluid, spray shaping is produced microspheric catalyst then
Embodiment four: the test of catalyst cracking vacuum residuum
Condition: heavy oil: grand celebration depressed heavy oil
Major equipment: fixed bed
Agent-oil ratio: 1: 1.2
Temperature of reaction: 466 ℃
Pressure: normal pressure
Result: cracked oil productive rate=83.88% (for depressed heavy oil, below identical)
Reacted gas productive rate=9.10% (therein ethylene 12.24W%, propylene 12.49W%)
Coking rate=7.02%
Embodiment five: the test of catalyst pyrolysis residue
Condition: heavy oil: grand celebration depressed heavy oil
Major equipment: fixed bed
Agent-oil ratio: 1.3: 1
Temperature of reaction: 490 ℃
Pressure: normal pressure
Result: cracked oil productive rate=22%
Splitting gas productive rate=60% (wherein triolefin and be 50.14W%, ethene 20.39W%, propylene 20.9W%)
Coking rate=18%
Claims (5)
1. the preparation method of a heavy oil cracking catalyst: the loess ore deposit is dried or dried, pulverize, sieve with 100 mesh sieve, remove impurity, Powdered loess ore deposit, water is heated to boiling after, add binding agent, stir fully that the dissolving back adds Powdered loess ore deposit, look after fully stirring evenly plasticity-and quantitatively; Extrusion molding is dried under 200-300 ℃ of condition, is contained in the high-temperature resistant container, at 600-700 ℃ of following secluding air, keeps sintering 2 hours; Stop heating, slowly cooling is taken out, and gets the fixed bed catalyst finished product.
2. the preparation method of a heavy oil cracking catalyst dries the loess ore deposit or dry, and is ground into the powdery granule of diameter 40 μ m with pulverizer; After water is heated to boiling, add A-S glue, stir, fully after the dissolving, add Powdered loess ore deposit, be made into flowable viscous fluid, sending spraying to be shaped then, microspherical catalyst.
3. the preparation method of heavy oil cracking catalyst according to claim 1; The fixed bed catalyst finished product of getting is beaten broken, porphyrize sieves with 200 mesh sieve, and undersized powder or powder sieve with 350 mesh sieve again, get the powder on the sieve, the fluid catalyst finished product.
4. according to the preparation method of claim 1 or 3 described heavy oil cracking catalysts; Binding agent is polyvinyl alcohol or A-S glue.
5. the preparation method of heavy oil cracking catalyst according to claim 1; High-temperature resistant container is a stainless steel tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97108204A CN1062006C (en) | 1997-09-02 | 1997-09-02 | Process for preparing heavy oil cracking catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97108204A CN1062006C (en) | 1997-09-02 | 1997-09-02 | Process for preparing heavy oil cracking catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1179462A true CN1179462A (en) | 1998-04-22 |
| CN1062006C CN1062006C (en) | 2001-02-14 |
Family
ID=5170224
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97108204A Expired - Fee Related CN1062006C (en) | 1997-09-02 | 1997-09-02 | Process for preparing heavy oil cracking catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1062006C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9187704B2 (en) * | 2001-07-31 | 2015-11-17 | Hitoshi Inoue | Method of biomass gasification |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1010707B (en) * | 1987-07-02 | 1990-12-05 | 三菱电机株式会社 | Separate type air conditioner |
| CN1007879B (en) * | 1987-07-13 | 1990-05-09 | 中国石化总公司石油化工科学研究院 | Cracking catalyst of clay molecular sieve with layer structure |
-
1997
- 1997-09-02 CN CN97108204A patent/CN1062006C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9187704B2 (en) * | 2001-07-31 | 2015-11-17 | Hitoshi Inoue | Method of biomass gasification |
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| Publication number | Publication date |
|---|---|
| CN1062006C (en) | 2001-02-14 |
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| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20010214 Termination date: 20110902 |