CN100389875C - For cracking C8Catalyst for fraction hydrogenation reaction, preparation method and application thereof - Google Patents
For cracking C8Catalyst for fraction hydrogenation reaction, preparation method and application thereof Download PDFInfo
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- CN100389875C CN100389875C CNB2006100990331A CN200610099033A CN100389875C CN 100389875 C CN100389875 C CN 100389875C CN B2006100990331 A CNB2006100990331 A CN B2006100990331A CN 200610099033 A CN200610099033 A CN 200610099033A CN 100389875 C CN100389875 C CN 100389875C
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Abstract
The invention discloses a method for cracking C8The fraction hydrogenation reaction catalyst comprises the following components: niaSibXc 1AldOxWherein X is1Is at least one element selected from the group consisting of elements of group IVB, Ni, Si and X1The element accounts for the weight percentage of the catalyst: ni 20-60%, Si 10-15%, X1Is 1-15%. The catalyst of the invention is prepared by mixing nickel, aluminum and X1Preparing aqueous solution from salt of group elements soluble in acid or water, adding raw material containing silicon element, titrating the mixed solution with alkali solution under the condition of fully stirring until the pH value is 7-8, filtering, drying and crushing the precipitate, adding nitric acid or/and phosphoric acid, sesbania gum and water, kneading, forming, drying and roasting to obtain the finished catalyst. Under certain inlet temperature, pressure, space velocity and hydrogen-oil molar ratio, the diolefin hydrogenation rate is greater than 85%. The catalyst of the invention overcomes the defects of high cost, low activity, easy poisoning, short operation period and the like of the existing noble metal catalyst. The catalyst is used in8In the hydrogenation of unsaturated hydrocarbons in the distillate.
Description
Technical field
The present invention relates to the catalyst of a kind of selective hydrogenation of diolefin as, monoene partial hydrogenation and preparation thereof, using method, purposes, particularly be applicable to cracking C
8Catalyst that the partial hydrogenation of cut selective hydrogenation of diolefin as, monoolefine is saturated and preparation thereof, using method, purposes.
Background technology
The production capacity of China's ethene increases substantially in recent years, and as the drippolene of cracking of ethylene accessory substance, its output is the 50-100% (wt) of ethylene production capacity.At present, the processed and applied of drippolene is roughly had two kinds of technologies, a kind of is directly full-cut fraction pyrolysis gasoline to be carried out hydrogenation without separation; Another kind is first separation of C
5 -And C
9 +, only to the C in the drippolene
6-C
8Cut is done aromatics extraction raw material behind two-stage hydrogenation.All ethylene units all will be used pyrolysis gasoline hydrogenation catalyst, and the demand of pyrolysis gasoline hydrogenation catalyst is very considerable, thereby both at home and abroad the developmental research of pyrolysis gasoline hydrogenation catalyst are paid much attention to.
For pyrolysis gasoline hydrogenation catalyst, the development of external catalyst technology is very fast.The pyrolysis gasoline hydrogenation catalyst trade mark seen of market has at home: LD-265, LD-365, Ho-22, PGC etc.Because domestic cracking stock is based on light diesel fuel and naphtha, external then in the majority with the high naphtha of lighter hydrocarbons and light component content, this has just caused the notable difference of single, double alkene content and distribution in the domestic and international pyrolysis gasoline cut fraction.The external relatively oil product of domestic oil product is heavier, when above-mentioned catalyst is used at home, all can not under design airspeed, satisfy long, completely, peace, steady, excellent running requirements.
Along with the reorganization and expansion of domestic ethylene project, the drippolene treating capacity increases, and former reactor can not satisfy the requirement that pyrolysis gasoline hydrogenation is handled, and part producer is for saving cost of investment, with C
8Cut separates back hydrogenation separately, to reclaim the aromatic hydrocarbons that wherein is rich in.Because the C after separating
8Fractional composition is concentrated, and heavy ends content is higher relatively, and impurity such as arsenic, water equal size are higher, and hydrotreatment is difficulty more, and the pyrolysis gasoline hydrogenation catalyst that was widely used originally can not satisfy C
8The requirement of the independent hydrogenation of cut.Need exploitation a kind of at C
8The catalyst of the independent hydrogenation of cut and appropriate processing condition.
Used pyrolysis gasoline hydrogenation catalyst on the present market, generally many is catalyst with noble metal such as Metal Palladium composition active material, but use cost is very high, especially rises period at noble metal scarcity of resources and price, and the use noble metal catalyst increases heavy burden economically; And noble metal catalyst is relatively stricter to the requirement of raw material oil product, and raw material well cuts such as arsenic, sulfur content is higher or moisturely all can make catalyst poisoning, causes the hydrogenation performance to descend, and the operation cycle obviously shortens.And the anti-poisoning capability of non-precious metal catalyst is strong, and ability arsenic, water-fast has overcome the deficiency of noble metal catalyst.
Can only prepare the catalyst of the base metal active component of low content with traditional dipping method, but activity is very low, can not satisfy cracking C
8The needs of cut fraction hydrogenation; And employing the method when active component content surpasses 20%, then because the filling of slaine significantly reduces the pore volume of catalyst carrier, specific area, makes catalyst activity reduction on the contrary, and the operation cycle is short; On the other hand, high-activity component content catalyst with immersion process for preparing, because the cooperative effect between each metallic element and the carrier element is poor, easily form the unordered accumulation of active component element, make in the catalyst roasting process migration that metallic element easily takes place, make grain growth, active, poor stability, no actual application value.
Summary of the invention
For solving traditional noble metal catalyst at cracking C
8Easily poison in the cut fraction hydrogenation, the deficiency of aspects such as the operation cycle is short, cost is high, poor stability, the inventor develops this catalyst through concentrating on studies.
The object of the present invention is to provide a kind of catalyst, especially for the catalyst of cracking cut fraction hydrogenation.It is mainly used in cracking C
8Cut unsaturated hydrocarbons and hydrogen carry out the reaction of hydrogenation, and making diene hydrogenation wherein is that monoolefine and part monoolefin hydrogenation are saturated hydrocarbons.Described cracking C
8Cut, its source in chemical industry mainly is to be that raw material carries out the accessory substance that thermal cracking is produced ethene and propylene with naphtha or light diesel fuel, can be that straight-chain hydrocarbons, branched-chain hydrocarbons and/or cyclic hydrocarbon or its have the hydro carbons of straight chain, side chain or ring structure, with and composition thereof, has unsaturated group, its unsaturated hydrocarbons can be the hydro carbons with thiazolinyl, alkynyl, and thiazolinyl can be conjugated diene or independent monoene, and main component is a styrene.
Catalyst of the present invention is the catalyst that base metal is formed.The catalyst that described base metal is formed is the catalyst of forming with base metal elements such as nickel; Be used in C
5-C
9Hydrodesulfurizationof of hydrocarbons is a secondary hydrogenation catalyst difference, also is different from general hydrodesulfurization, denitrogenation or takes off other impurity, as hydrorefined catalyst such as arsenic, vanadium metal and antimony.
Catalyst of the present invention has not only reduced production cost, has also got rid of the harmful effect to the hydrogenation performance generation of noble metal catalyst such as arsenic, sulphur and water simultaneously, and market potential is huge, remarkable in economical benefits.
Another object of the present invention is to provide a kind of aforementioned Preparation of catalysts method.
A further object of the present invention is to provide a kind of aforementioned catalyst at cracking C
8Application in the cut fraction hydrogenation reaction.
A kind of cracking cut fraction hydrogenation catalyst formula composed as follows that is used for of the present invention:
Ni
aSi
bX
1 cAl
dO
x
Wherein Ni is a nickel; Si is a silicon, X
1Be at least a element that is selected from the IVB family element set, especially preferably zirconium (Zr) and/or titanium (Ti) element, Al is an aluminium, O is an oxygen; A, b and c are Ni, Si and X
1It is 20-60% that element accounts for the weight percent content of catalyst: a, is preferably 40%; B is 10-15%, is preferably 12.5%; C is 1-15%, is preferably 8%; D, x are the numbers that Al and O satisfy above each element oxidation valence state.
Preparing the contained coherent element raw material of catalyst of the present invention not limited by its kind.Any oxide that contains the coherent element component or the compound that produces oxide when calcining can be used, as produce hydroxide, metal acid, nitrate, carbonate, ammonium salt, acetate and the formates etc. of oxide when calcining, or the compound that contains the component of two kinds or multiple element listed above equally also can use.
The raw material of nickel element can be compound or its mixtures such as nickel oxide, nickel hydroxide, nickel nitrate, nickelous carbonate, basic nickel carbonate, nickel formate or nickel acetate in the catalyst; The raw material of element silicon can be compound or its mixtures such as silica gel, silicic acid, Ludox, silicon powder or zirconium silicate; X
1Be to be selected from IVB family element, for example the raw material of zr element can be compound or its mixtures such as zirconia, zirconium hydroxide, zirconium nitrate, zirconium silicate or zirconium oxychloride; The raw material of titanium elements can be compound or its mixtures such as titanium dioxide or titanyl nitrate; The raw material of aluminium element can be compound or its mixtures such as aluminum nitrate or aluminium chloride.
Preparation of catalysts method of the present invention is to contain the compound co-precipitation of each component element, in conjunction with the method for machinery kneading.With nickel, aluminium, X
1Water-soluble salt of family's salt is made into the aqueous solution, and nickel salt is 100 parts by weight, and aluminium salt is 20-50 part, is preferably 30 parts, X
1Family's salt is 1-20 part, is preferably 10 parts, dissolves fully with salpeter solution, add the raw material that 2-20 part contains element silicon, being preferably 15 parts, is 7-8 with the above-mentioned mixed solution of aqueous slkali titration to PH under abundant stirring condition, suction filtration, drying precipitate, pulverize that the back adds nitric acid or/and phosphoric acid, sesbania gum, water are mediated, moulding, at 100-120 ℃, preferred 110 ℃ of dry 4-6 hour, preferred 5 hours, 500-700 ℃, preferred 600 ℃ of roasting 4-6 hours, obtained finished catalyst in preferred 5 hours.It is 20-60% for the Ni element that catalyst is respectively formed content, preferred 40%; The Si element is 10-15%, preferred 12.5%; X
1Family's element is 1-15%, preferred 8%.
There is no particular limitation for shaping of catalyst of the present invention, can be spherical, cylindrical, annular or other is special-shaped as the cloverleaf pattern particle.Preferably be shaped to the annular and other as abnormity such as clover.The diameter of granular size or length are at 1-10mm, preferably at 2-8mm, particularly preferably in 2.5-6.0mm.
Catalyst of the present invention is applicable to cracking C
8The catalytic hydrogenation reaction of unsaturates in the cut, cracking C
8Cut unsaturates content, if with bromine valency (carrying out the index that degree of unsaturation in the organic compound or quantity are demarcated in the stoichiometry addition reaction) expression with simple substance bromine, may be in the scope of 100 gram bromines/100 gram oil at 30 gram bromines/100 gram oil; Cracking C
8The cut diene content, promptly if diene value with iodine value (carrying out the index that alkadienes quantity in the organic compound is demarcated in the stoichiometry addition reaction with iodine) expression, may restrain oil in the scope of 30 gram iodine/100 gram oil in 10 gram iodine/100.
Catalyst of the present invention adopts the adiabatic reactor reactor to carry out catalytic hydrogenation reaction, and the process conditions of employing are: the feed(raw material)inlet temperature is 80-150 ℃, preferred 100 ℃; Reaction pressure is 2.0-6.0Mpa, preferred 4Mpa; The green oil air speed is 1.5-2.5h
-1, preferred 2.0h
-1Hydrogen/oil mol ratio is 0.5-2.0, preferred 1.2.Can reach good hydrogenation result in this process conditions scope, the diene value of hydrogenated products oil is less than 2.0 gram iodine/100 gram oil, and the diene hydrogenation rate is greater than 85%.
It is to be noted: be used for cracking of ethylene accessory substance C
5-C
9The noble metal of cut fraction section hydrogenation such as the catalyst of palladium carry out in the adiabatic reactor reactor industrial normally being seated in, and have nothing different with the suitable adiabatic reactor reactor that adopts of catalyst of the present invention, also promptly so long as be used for cracking of ethylene accessory substance C
5-C
9The reactor of cut fraction section hydrogenation substitutes noble metal catalyst with catalyst of the present invention, just selects the hydrogenation technique condition of suitable catalyst of the present invention, and the hydrogenation purpose that reaches expectation gets final product, and need not newly-built or changes special reactor and can realize.
Catalyst hydrogenation excellent performance of the present invention, the hydrogenation performance of described catalyst under the process conditions of suitable catalyst of the present invention, reaches the cracking C that general use noble metal catalyst will contain unsaturated hydrocarbons
8Cut and hydrogen carry out the same good effect of hydrogenation.
The specific embodiment:
The following examples can make those skilled in the art more fully understand the present invention, but do not limit the present invention in any way.
This patent has been invented a kind of method for preparing catalyst of uniqueness, agents useful for same in the following example, and if no special instructions, it is pure that the agents useful for same grade is analysis.
NH
4HCO
3Solution: weigh 400g NH
4HCO
3, dissolve fully with 4000ml distilled water;
Ammonia spirit: analyze pure.
Embodiment 1 Preparation of catalysts of the present invention
Taking by weighing 100 weight portion nickel nitrates, 30 weight portion aluminum nitrates, 10 weight portion zirconium oxychlorides dissolves fully with salpeter solution, add 15 weight portion silicon powders, under abundant stirring condition with ammonia water titration as above mixed solution equal 7 to PH, suction filtration, drying precipitate, pulverizing back add nitric acid, phosphoric acid, sesbania gum, water kneading, moulding, obtained finished catalyst in 5 hours in 5 hours, 600 ℃ roastings of 110 ℃ of dryings, catalyst is respectively formed content for the Ni element is 40%, the Si element is 12.5%, zr element is 8%.
Embodiment 2 Preparation of catalysts of the present invention
Taking by weighing 100 weight portion nickel nitrates, 50 weight portion aluminum nitrates, 1 weight portion zirconium oxychloride dissolves fully with salpeter solution, add 2 weight portion silicon powders, under abundant stirring condition with ammonia water titration as above mixed solution equal 8 to PH, suction filtration, drying precipitate, pulverize the back and add nitric acid, phosphoric acid, sesbania gum, water kneading, moulding, 6 hours, 500 ℃ roastings of 100 ℃ of dryings and obtained finished catalyst in 6 hours, catalyst is respectively formed content for the Ni element is 20%, the Si element is 10%, zr element is 1%.
Embodiment 3 Preparation of catalysts of the present invention
Taking by weighing 100 weight portion nickel nitrates, 20 weight portion aluminum nitrates, 20 weight portion zirconium oxychlorides dissolves fully with salpeter solution, add 20 weight portion silicon powders, under abundant stirring condition with ammonia water titration as above mixed solution equal 7 to PH, suction filtration, drying precipitate, pulverize the back and add nitric acid, sesbania gum, water kneading, moulding, 4 hours, 700 ℃ roastings of 120 ℃ of dryings and obtained finished catalyst in 4 hours, catalyst is respectively formed content for the Ni element is 60%, the Si element is 15%, zr element is 15%.
Embodiment 4 Preparation of catalysts of the present invention
Take by weighing 100 weight portion nickel formates, nickel acetate mixture, 25 weight portion aluminium chloride, 10 parts by weight of titanium dioxide are dissolved fully with salpeter solution, add 13 weight portion silica gel, are fully using NH under the stirring condition
4HCO
3Solution titration as above mixed solution equals 8 to PH, suction filtration, drying precipitate, pulverizing, add nitric acid, phosphoric acid, sesbania gum, water kneading, moulding, 4 hours, 700 ℃ roastings of 100 ℃ of dryings and obtained finished catalyst in 6 hours, catalyst is respectively formed content for the Ni element is 47%, the Si element is 13%, titanium elements is 12.8%.
Embodiment 5 Preparation of catalysts of the present invention
Take by weighing 100 weight portion basic nickel carbonates, 28 weight portion aluminium chloride, 18 weight portion zirconium hydroxides, titanyl nitrate mixture, dissolve fully, add 19 weight portion silanes, silica mixture, fully using NH under the stirring condition with salpeter solution
4HCO
3Solution titration as above mixed solution equals 7 to PH, suction filtration, drying precipitate, pulverizing, add nitric acid, phosphoric acid, sesbania gum, water kneading, moulding, 4 hours, 500 ℃ roastings of 120 ℃ of dryings and obtained finished catalyst in 4 hours, catalyst is respectively formed content for the Ni element is 33%, the Si element is 15%, zirconium, titanium elements are 10%.
The using method of embodiment 6 catalyst of the present invention
Catalyst of the present invention: preparation is with embodiment 1
Catalyst of the present invention can adopt the adiabatic reactor reactor to carry out C
8The catalytic hydrogenation reaction of cut, reaction result under following hydroconversion condition such as following table:
| Inlet temperature (℃) | Pressure (MPa) | Green oil air speed (h 1) | Hydrogen/oil mol ratio | Raw material diene (gI/100g) | Product diene (gI/100g) | Hydrogenation rate (%) |
| 80 | 2.0 | 1.5 | 0.5 | 9.23 | 1.38 | 85.0 |
The using method of embodiment 7 catalyst of the present invention
Catalyst of the present invention: preparation is with embodiment 2
Catalyst of the present invention can adopt the adiabatic reactor reactor to carry out C
8The catalytic hydrogenation reaction of cut, reaction result under following hydroconversion condition such as following table:
| Inlet temperature (℃) | Pressure (MPa) | Green oil air speed (h 1) | Hydrogen/oil mol ratio | Raw material diene (gI/100g) | Product diene (gI/100g) | Hydrogenation rate (%) |
| 110 | 4.0 | 2.0 | 1.2 | 9.23 | 0.85 | 90.8 |
The using method of embodiment 8 catalyst of the present invention
Catalyst of the present invention: preparation is with embodiment 3
Catalyst of the present invention can adopt the adiabatic reactor reactor to carry out C
8The catalytic hydrogenation reaction of cut, reaction result under following hydroconversion condition such as following table:
| Inlet temperature (℃) | Pressure (MPa) | Green oil air speed (h 1) | Hydrogen/oil mol ratio | Raw material diene (gI/100g) | Product diene (gI/100g) | Hydrogenation rate (%) |
| 150 | 6.0 | 2.5 | 2.0 | 9.23 | 0.62 | 93.3 |
The rerum natura of catalyst of the present invention and imported L D-265 catalyst relatively
The rerum natura of table 1 catalyst of the present invention and imported L D-265 catalyst relatively
| Catalyst | Catalyst of the present invention | LD-265 |
| Outward appearance, size (mm) | φ 2.8-3.0 abnormity, black | φ 2 * 4 spherical drabon looks |
| Main active component | Ni | Palladium |
| Carrier | γ-Al 2O 3 |
As known from Table 1, the rerum natura of catalyst of the present invention is different from external catalyst, and its main active component is also different, and external catalyst master active component is a precious metal palladium, and catalyst master active component of the present invention is a nickel.
For showing that catalyst of the present invention is at cracking C
8Beneficial effect in the cut hydrogenation reaction of unsaturated hydrocarbon, further set forth beneficial effect of the present invention below by Comparative Examples:
Comparative Examples 1
Catalyst of the present invention: the preparation method is with embodiment 4
Contrast medium 1:(imported L D-265)
| CAT | Inlet temperature (℃) | Pressure (MPa) | Green oil air speed (h 4) | Hydrogen/oil mol ratio | Raw material diene (gI/100g) | Product diene (gI/100g) | Hydrogenation rate (%) |
| The present invention | 80 | 3.0 | 2.0 | 0.6 | 9.23 | 1.05 | 88.6 |
| LD-265 | 80 | 3.0 | 2.0 | 0.6 | 9.23 | 1.88 | 79.6 |
Conclusion: as seen from the above table, at cracking C
8In the cut hydrogenation reaction of unsaturated hydrocarbon, the hydrogenation activity of catalyst of the present invention is higher than imported L D-265 catalyst.
Comparative Examples 2
Catalyst of the present invention: the preparation method is with embodiment 5
Contrast medium 2:(tradition infusion process)
With mixer kneader such as the aluminium hydrate powder of nitrate method or Carbonization Preparation and aqueous solution of nitric acid, water, behind the extruded moulding, 100 ℃ of oven dry, 800 ℃ of roastings are 6 hours then, comparative catalyst's carrier.Take by weighing the pure nickel nitrate of a certain amount of analysis, the adding distil water dissolving, the overall solution volume amount is controlled to be 1.05 times of carrier water absorption.Solution poured into uninterruptedly stirs 15 minutes in the carrier, 100 ℃ of oven dry, 500 ℃ of roastings 6 hours, the comparative catalyst, nickel content is 20% among the comparative catalyst.
| CAT | Inlet temperature (℃) | Pressure (MPa) | Green oil air speed (h 4) | Hydrogen/oil mol ratio | Raw material diene (gI/100g) | Product diene (gI/100g) | Hydrogenation rate (%) |
| The present invention | 100 | 3.5 | 2.5 | 0.8 | 9.23 | 0.70 | 92.4 |
| Contrast medium 2 | 100 | 3.5 | 2.5 | 0.8 | 9.23 | 1.27 | 86.2 |
Conclusion: as seen from the above table, catalyst of the present invention is at cracking C
8Hydrogenation activity in the cut hydrogenation reaction of unsaturated hydrocarbon is higher than the comparative catalyst.
The foregoing description 6,7,8, and in the Comparative Examples 1,2, used catalyst of the present invention no matter it needs only its component, content within the scope of the present invention with which kind of method preparation, all has essentially identical experiment effect and purposes.
Claims (17)
1. one kind is used for cracking C
8The cut fraction hydrogenation catalysts is characterized in that: consist of Ni
aSi
bX
1 cAl
dO
x,
Wherein Ni is a nickel, and Si is a silicon, X
1Be at least a element that is selected from the IVB family element set, Al is an aluminium, and O is an oxygen, and a, b and c are Ni, Si and X
1Element accounts for the weight percent content of catalyst, and a is 20-60%, and b is 10-15%, and c is 1-15%, and d, x are the numbers that Al and O satisfy above each element oxidation valence state.
2. catalyst according to claim 1 is characterized in that: described Ni, Si and X
1The weight percent content a that element accounts for catalyst is that Ni is 40%, and b is that Si is 12.5%, and c is X
1Be 8%.
3. catalyst according to claim 1 is characterized in that: described element X
1Be a kind of of zirconium (Zr) element, titanium (Ti) element or two kinds.
4. catalyst according to claim 1 is characterized in that: the raw material of described nickel element is nickel oxide, nickel hydroxide, nickel nitrate, nickelous carbonate, basic nickel carbonate, nickel formate, nickel acetate or its mixture.
5. catalyst according to claim 1 is characterized in that: the raw material of described element silicon is silica gel, Ludox, silicon powder and zirconium silicate or its mixture; Described aluminium element raw material is aluminium chloride, aluminum nitrate or its mixture.
6. catalyst according to claim 3 is characterized in that: the raw material of described zr element is zirconia, zirconium hydroxide, zirconium nitrate, zirconium silicate, zirconium oxychloride or its mixture.
7. catalyst according to claim 3 is characterized in that: the raw material of described titanium elements is titanium dioxide, titanyl nitrate or its mixture.
8. the described Preparation of catalysts method of claim 1 is characterized in that step is:
1) will contain nickel, aluminium, X
1The salt that dissolves in acid or water of family's element is made into the aqueous solution, and nickel salt is 100 parts by weight, and aluminium salt is 20-50 part, X
1Family's salt is 1-20 part;
2) adding the raw material that 2-20 part contains element silicon, is 7-8 with the above-mentioned mixed solution of aqueous slkali titration to PH under abundant stirring condition, and suction filtration, pulverizes that the back adds nitric acid or/and phosphoric acid, sesbania gum, water kneading, moulding at drying precipitate;
3) at 100-120 ℃ of dry 4-6 hour;
4) 500-700 ℃ obtained finished catalyst in roasting 4-6 hour.
9. Preparation of catalysts method according to claim 8, its spy just is: the salt of aluminium described in the step 1) is 30 parts, described X
1Family's salt is 10 parts.
10. Preparation of catalysts method according to claim 8 is characterized in that step 2) described in silicon content be 15 parts.
11. Preparation of catalysts method according to claim 8 is characterized in that, described step 3) is 110 ℃ of dryings 5 hours.
12. Preparation of catalysts method according to claim 8 is characterized in that described step 4) is for to obtain finished catalyst in 5 hours 600 ℃ of following roastings.
13. the described catalyst of claim 1 is at cracking C
8Application in the cut fraction hydrogenation reaction, it is characterized in that process conditions are: the feed(raw material)inlet temperature is 80-150 ℃, preferred 100 ℃; Reaction pressure is 2.0-6.0Mpa, preferred 4.0Mpa; The green oil air speed is 1.5-2.5h
-1, preferred 2.0h
-1Hydrogen/oil mol ratio is 0.5-2.0, preferred 1.2.
14. application according to claim 13 is characterized in that, described feed(raw material)inlet temperature is 100 ℃.
15. application according to claim 13 is characterized in that, described reaction pressure is 4.0Mpa.
16. application according to claim 13 is characterized in that, described green oil air speed is 2.0h
-1
17. application according to claim 13 is characterized in that, described hydrogen/oil mol ratio is 1.2.
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|---|---|---|---|
| CNB2006100990331A CN100389875C (en) | 2006-07-14 | 2006-07-14 | For cracking C8Catalyst for fraction hydrogenation reaction, preparation method and application thereof |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1255479A (en) * | 1998-09-16 | 2000-06-07 | 奥克森诺奥勒芬化学股份有限公司 | Process for preparing high-grade carbonyl synthetic alohol after two-staged hydrogenation formoxyl from alkene mixture |
| US6245221B1 (en) * | 1997-08-22 | 2001-06-12 | Exxon Research And Engineering Company | Desulfurization process for refractory organosulfur heterocycles |
| CN1358701A (en) * | 2000-12-14 | 2002-07-17 | 奥克森诺奥勒芬化学股份有限公司 | Hydrogenation method for hydroformylation mixture |
| US20030073874A1 (en) * | 2001-10-15 | 2003-04-17 | Michael Koch | Process for catalytic hydrogenation |
-
2006
- 2006-07-14 CN CNB2006100990331A patent/CN100389875C/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6245221B1 (en) * | 1997-08-22 | 2001-06-12 | Exxon Research And Engineering Company | Desulfurization process for refractory organosulfur heterocycles |
| CN1255479A (en) * | 1998-09-16 | 2000-06-07 | 奥克森诺奥勒芬化学股份有限公司 | Process for preparing high-grade carbonyl synthetic alohol after two-staged hydrogenation formoxyl from alkene mixture |
| CN1358701A (en) * | 2000-12-14 | 2002-07-17 | 奥克森诺奥勒芬化学股份有限公司 | Hydrogenation method for hydroformylation mixture |
| US20030073874A1 (en) * | 2001-10-15 | 2003-04-17 | Michael Koch | Process for catalytic hydrogenation |
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