CN1049679C - Catalyst for hydrogenation conversion of diesel - Google Patents
Catalyst for hydrogenation conversion of diesel Download PDFInfo
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Abstract
The present invention relates to a hydrogenating conversing catalyst for diesel oil. A carrier is composed of aluminum oxide and an unformed silicon aluminum molecular sieve. Hydrogenizing metal components can be at least one metal W or Mo of the VIB group and at least one metal Ni or Co of the VIII group. The present invention is suitable for the hydrogenation conversion of petroleum distillate with the temperature of 150 to 400 DEG C, and is especially suitable for the conversion of catalytic cracking light cycle oil (LCO) of which the sulfur content, the nitrogen content and the aromatic content are high and the cetane value is low. The present invention is characterized in that the sulfur content, the nitrogen content and the aromatic content are lowered under moderate conditions, and the cetane value of the product is enhanced substantially.
Description
The present invention relates to a kind of catalyst for hydrocracking diesel oil.
Along with heavy oil, the widespread use of residual oil processing technology has increased gasoline, the source of light-end products such as diesel oil, but the fraction of diesel oil foreign matter content height that obtains thus, and the storage stability is poor, and cetane value is low, needs further processing just can obtain qualified product.With the heavy oil fluid catalytic cracking is the coking that comprises of representative, poor ignition quality fuels such as thermally splitting diesel oil, be characterized in content of heteroatoms height such as sulphur, nitrogen, the aromaticity content height, cetane value is low, and the storage stability is poor, be starved of a kind of heteroatomss such as sulphur, nitrogen that can remove and satisfy the environmental regulation requirement, improve the storage stability, can increase substantially cetane value again, satisfy the novel method that quality product requires.
US5219814, US4820403, US4971680 etc. have introduced a kind of method of using hydrocracking technology to handle LCO, its common feature is＜180 ℃ of cracking conversion rates of control, produces high-octane petroleum naphtha, desulfurization simultaneously, impurity such as nitrogen, the diesel oil of by-product high hexadecane value, but that its shortcoming is the yield of diesel oil is low, is unfavorable for that the countries and regions of diesel fuel oil shortage are used; Simultaneously, because its product cracking degree height, the hydrogen consumption is big, has hindered in the refinery of hydrogen supply anxiety and has promoted and use.
US5068025, US4619759, US5110444, WO9426846 etc. have introduced a kind of use hydrogenating desulfurization, the technology of hydrogenation aromatics-removing, its common feature is first section hydrogenating desulfurization, impurity such as nitrogen, second section is reduced aromaticity content significantly by degree of depth aromatic hydrogenation saturated reaction, and the cetane value of its product is greatly improved simultaneously, but its shortcoming is the operational condition harshness, need more high pressure or use noble metal catalyst, therefore operation and investment cost are huge, simultaneously because the degree of saturation height of product, the hydrogen consumption is big, is unfavorable for promoting and utilizing.
Though use general Hydrobon catalyst can improve the character of poor ignition quality fuel, reduce heteroatomic content such as sulphur, nitrogen, improve its storage stability, but cetane value amplification is little, generally be no more than 5 units, need the diesel oil of a large amount of high hexadecane values to be in harmonious proportion with it, or use ignition dope to reach the quality product requirement, this will bring the reduction and the increase expense of product grade.
The invention provides a kind of hydrogenation conversion catalyst, described catalyzer is a kind of dual function hydrogenation catalyst.Its theoretical foundation is to make the condensed-nuclei aromatics fractional saturation that cetane value is lower in the diesel component, and open loop becomes the mononuclear aromatics of band side chain, thereby significantly increases the cetane value of product; Its key problem in technology is the selective opening of catalyzer to condensed-nuclei aromatics, owing to select for use molecular sieve component as the selective opening component, consider oxygen in the poor ignition quality fuel, content of heteroatoms height such as nitrogen require selected molecular sieve that good hydrothermal stability and anti-nitrogen poisoning capability and suitable pore structure must be arranged.Require simultaneously that each component has suitable proportioning in the catalyzer, guarantee that catalyzer has very high heteroatomic abilities such as desulfurization nitrogen, and long running period.Described catalyzer can be at similar to the general Hydrobon catalyst heteroatomss such as sulphur, nitrogen that remove, when improving its storage stability, and the cetane value of raising product by a larger margin; Than raw material, the cetane value of product can increase by 10 more than the unit.Because this technology is low than hydrocracking technology cracking degree, and is low than hydrogenation dearomatization technology degree of saturation, therefore can reduce product hydrogen consumption, the operational condition of this catalyzer relaxes simultaneously, is similar to general hydrotreatment, and it is big to have treatment capacity, and hydrogen consumes advantages such as low.
Described catalyzer is a kind of dual function hydrogenation catalyst, its hydrogenation metal component can be the combination of at least a group vib metal oxide or sulfide and at least a VIII family's group metal oxide or sulfide, the salic 40w%-90w% of carrier, amorphous silicon aluminium 0-20w%, molecular sieve 5w%-40w%.
In the described carrier salic be that a kind of crystalline phase is the aluminum oxide of pseudo-boehmite, content 40w%-90w%.
The sieve and silica-sesquioxide weight ratio 1 of contained amorphous silicon aluminium: 2-2 in the described carrier: 1, content 0-20w%, preferably 10w%-20w%.
Contained molecular sieve can be a y-type zeolite in the described carrier, and preferably the macropore y-type zeolite is characterized in pore volume 0.4-0.52ml/g, specific surface (BET) 750-900m
2/ g, lattice constant 2.420-2.500nm, relative crystallinity 90-110%, SiO
2/ Al
2O
3Than 7-15, content 5w%-40w%, preferably 10w%-30w%.
The type shape of described carrier can be sheet, and is spherical, strip, diameter 1.0mm-3.0mm preferably, the strip of length 3.0mm-8.0mm.
Described hydrogenation metal can be the combination of at least a group vib metal oxide or sulfide and at least a VIII family metal oxide or sulfide, and the group vib metal can be Mo or W, preferably selects W for use, content 10w%-30w%.VIII group metal can be Ni or Co, preferably selects Ni for use, content 2w%-15w%.
Described hydrogenation metal can add by the method for dipping respective metal salts solution after respective metal salt and carrier component kneading and compacting or the carrier moulding.Mo salt can be selected solubility molybdenum oxide or ammonium molybdate for use, and W salt can be selected ammonium metawolframate or wolframic acid for use, but Ni salt can be selected decomposing N i salt such as nickelous nitrate, nickelous carbonate for use, and Co salt can select for use Xiao Suangu, cobaltous carbonate etc. can decompose Co salt.
Adopt the catalyzer of the present invention can be, pressure 4.0-8.0MPa, liquid air speed 1.0-3.0h at temperature of reaction 340-400 ℃
-1, processing poor ignition quality fuel under the condition of hydrogen to oil volume ratio 400-1500, it can be at similar to the general Hydrobon catalyst heteroatomss such as sulphur, nitrogen that remove, when improving its storage stability, the cetane value of raising product by a larger margin; The cetane value of product can increase by 10 more than the unit, and diesel yield is greater than 95%.The poor ignition quality fuel of being processed can be sulphur content 0.05w%-2.5w%, the catalytic cracking light cycle oil (catalytic cracking diesel oil) of nitrogen content 100 μ g/g-1500 μ g/g.
Below further specify characteristics of the present invention by example:
Example 1
Getting high purity aluminium oxide SB powder that macroporous aluminium oxide 400g that Fushun Petrochemical Company oil three factories produce and the hydrolysis of 100g aluminium alcoholates make, to add the 250ml weight percent concentration be that tackiness agent (hereinafter to be referred as tackiness agent) that 10% nitric acid peptization makes mixes and pinches, adding water becomes can squeeze paste, extruded moulding, 110 ℃ of dryings, 550 ℃ of roastings 4 hours are with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyst A.
Example 2
Get the macroporous aluminium oxide 250g that oil three factories produce, sial 150g (sieve and silica-sesquioxide weight ratio 1: 1) mixes with the 100g tackiness agent and pinches, adding water becomes can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours are with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyst B.
Example 3
Get the macroporous aluminium oxide 250g that oil three factories produce, USY zeolite (ultrastable Y, pore volume 0.36ml/g, lattice constant 2.550nm, specific surface 710
2/ g, relative crystallinity 76%, SiO
2/ Al
2O
3Than 5.33) 150g mixes with the 100g tackiness agent and pinches, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours get catalyzer C.
Example 4
Get the macroporous aluminium oxide 250g that oil three factories produce, the DAY zeolite is (through peracid extracting ultrastable Y, pore volume 0.38ml/g, specific surface 650
2/ g, lattice constant 2.432nm, relative crystallinity 57%, SiO
2/ Al
2O
3Than 7.3) 150g mixes with the 100g tackiness agent and pinches, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours get catalyzer D.
Example 5
Get the macroporous aluminium oxide 250g that oil three factories produce, MPY zeolite (y-type zeolite, pore volume 0.46ml/g, specific surface 810
2/ g, lattice constant 2.442nm, relative crystallinity 95%, SiO
2/ Al
2O
3Than 11.2) 150g mixes with the 100g tackiness agent and pinches, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours get catalyzer E.
Example 6
Get the macroporous aluminium oxide 200g that oil three factories produce, MPY zeolite 200g and 100g tackiness agent mix and pinch, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours are with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyzer F.
Example 7
Get the macroporous aluminium oxide 300g that oil three factories produce, MPY zeolite 100g and 100g tackiness agent mix and pinch, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours are with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyzer G.
Example 8
Get the macroporous aluminium oxide 350g that oil three factories produce, MPY zeolite 50g and 100g tackiness agent mix and pinch, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours are with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyzer H.
Example 9
Get the macroporous aluminium oxide 250g that oil three factories produce, MPY zeolite 100g, sial 50g and 100g tackiness agent mix and pinch, add water and become to squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, steeping fluid dipping with ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyst I.
Example 10
Get the macroporous aluminium oxide 250g that oil three factories produce, MPY zeolite 75g, sial 75 mixes with the 100g tackiness agent and pinches, add water and become to squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, steeping fluid dipping with ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours, catalyzer J.
Example 11
Get the macroporous aluminium oxide 250g that oil three factories produce, MPY zeolite (y-type zeolite, pore volume 0.438ml/g, specific surface 828
2/ g, lattice constant 2.445nm, relative crystallinity 95%, SiO
2/ Al
2O
3Than 8.17) 75g, sial 75g and 100g tackiness agent mix and pinch, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours get catalyzer K.
Example 12
Get the macroporous aluminium oxide 250g that oil three factories produce, MPY zeolite (y-type zeolite, pore volume 0.502ml/g, specific surface 840
2/ g, lattice constant 2.439nm, relative crystallinity 96%, SiO
2/ Al
2O
3Than 12.3) 75g, sial 75g and 100g tackiness agent mix and pinch, and add water and become can squeeze paste, 110 ℃ of dryings of extruded moulding, 550 ℃ of roastings 4 hours, with the steeping fluid dipping of ammonium metawolframate and nickelous nitrate preparation, 110 ℃ of dryings, 500 ℃ of roastings 4 hours get catalyzer L.
Comparative example 1
A kind of industrial diesel oil Hydrobon catalyst M (a kind of catalyzer that contains W-Mo-Ni-P).The composition of each catalyzer of table 1.:
| Catalyzer | A | B | C | D | E | F | G | H | I | J | K | L |
| Form w% | ||||||||||||
| WoO 3 | 22.1 | 22.2 | 22.0 | 22.0 | 22.1 | 22.3 | 22.1 | 22.2 | 21.8 | 22.2 | 18.9 | 25.3 |
| NiO | 6.2 | 6.0 | 6.1 | 7.3 | 6.2 | 6.2 | 6.3 | 6.0 | 6.0 | 6.3 | 6.0 | 4.8 |
| Carrier is formed w% | ||||||||||||
| USY | 30 | |||||||||||
| MPY | 30 | 40 | 20 | 10 | 20 | 15 | 15 | 15 | ||||
| Sial | 30 | 10 | 15 | 15 | 15 | |||||||
| γ-Al 2O 3 | 100 | 70 | 70 | 70 | 70 | 60 | 80 | 90 | 70 | 70 | 70 | 70 |
| DAY | 30 | |||||||||||
Table 2. stock oil character: density (20 ℃), g/cm
30.9123 sulphur, μ g/g 3564 nitrogen, μ g/g 850 cetane value 30 boiling ranges (ASTM D976), ℃ 10% 23330% 25550% 27470% 30690% 353EBP 360
Catalyst breakage becomes 20-40 purpose particle, measure the 6ml catalyzer with the quartz sand mixing of the corresponding granularity of the two volumes reactor of packing into, with the kerosene sulfuration that contains 1% dithiocarbonic anhydride, sulfuration is back control reaction conditions fully: table 3. reaction conditions: temperature of reaction, ℃ 360 volume space velocities, h
-11.5 reaction pressure, MPa 6.0 hydrogen to oil volume ratio, 800 table 4. reaction results and product property (40 hours):
| Catalyzer | A | B | C | D | E | F | G | H | I | J | K | L | M |
| Product property | |||||||||||||
| Density d 4 20，g/cm | 0.8906 | 0.8879 | 0.8782 | 0.8791 | 0.8733 | 0.8702 | 0.8755 | 0.8789 | 0.8743 | 0.8753 | 0.8851 | 0.8750 | 0.8755 |
| Sulphur, μ g/g | 300 | 220 | 100 | 82 | 78 | 63 | 113 | 163 | 80 | 91 | 163 | 70 | 153 |
| Desulfurization degree | 91.6 | 93.8 | 97.2 | 97.7 | 97.8 | 98.2 | 96.8 | 95.4 | 97.7 | 97.4 | 95.4 | 98.0 | 95.7 |
| Nitrogen, μ g/g | 54.3 | 29.1 | 10.1 | 9.2 | 2.7 | 2.1 | 6.7 | 9.8 | 3.3 | 3.5 | 7.1 | 3.3 | 11.2 |
| Denitrification percent | 93.91 | 96.6 | 98.8 | 98.8 | 99.6 | 99.8 | 99.2 | 98.8 | 99.6 | 99.6 | 99.0 | 99.6 | 98.7 |
| Cetane value | 33.1 | 34.2 | 39.2 | 38.3 | 43.1 | 44.3 | 42.5 | 40.1 | 42.7 | 42.3 | 40,8 | 42.1 | 34.8 |
| Cetane value amplification | 3.1 | 4.2 | 9.2 | 8.3 | 13.1 | 14.3 | 12.5 | 10.1 | 12.7 | 12.3 | 10.8 | 12.1 | 4.8 |
| Less than 180 ℃ of yields, w% | 0.7 | 1.1 | 3.7 | 3.0 | 3.8 | 4.9 | 3.1 | 2.1 | 3.3 | 3.1 | 2.7 | 3.1 | 1.6 |
By table 4. as can be seen, by in catalyzer, adding the cetane value that molecular sieve can obviously improve product, and the cetane value amplification of selecting different its products of molecular sieve for use has very big difference, adopts the cetane value amplification maximum of its product of catalyzer of molecular sieve of the present invention.Table 5. reaction result and product property (200 hours):
Table 6. reaction result and product property (1000 hours):
Annotate: desulfurization degree calculates by following formula: 100 * (feed sulphur content-product sulphur content)/feed sulphur content
| Catalyzer | A | B | C | D | E | F | G | H | I | J | M |
| Product property | |||||||||||
| Density (20 ℃), g/cm 3 | 0.8916 | 0.8878 | 0.8858 | 0.8807 | 0.8812 | 0.8800 | 0.8820 | 0.8830 | 0.8808 | 0.8810 | 0.8857 |
| Sulphur, μ g/g | 305 | 241 | 220 | 163 | 117 | 93 | 134 | 171 | 110 | 108 | 157 |
| Desulfurization degree | 91.4 | 93.2 | 93.8 | 95.3 | 96.7 | 97.3 | 96.2 | 95.2 | 96.9 | 97.0 | 95.6 |
| Nitrogen, μ g/g | 61.3 | 33.4 | 30.1 | 13.0 | 9.7 | 8.9 | 11.3 | 15.6 | 9.6 | 8.9 | 13.1 |
| Denitrification percent | 92.8 | 96.1 | 96.4 | 98.5 | 98.9 | 99.0 | 98.7 | 98.2 | 98.9 | 99.0 | 98.5 |
| Cetane value | 33.5 | 34.2 | 35.7 | 37.7 | 40.3 | 41.0 | 39.5 | 38.9 | 40.6 | 40.3 | 34.6 |
| Cetane value amplification | 3.5 | 4.2 | 5.7 | 7.7 | 10.3 | 10.2 | 9.5 | 8.9 | 10.6 | 10.3 | 4.6 |
| Less than 180 ℃ of yields, w% | 0.6 | 1.2 | 2.1 | 2.1 | 3.1 | 3.1 | 2.5 | 2.2 | 3.0 | 2.9 | 1.6 |
| Catalyzer | C | D | E | H | I | J | M |
| Product property | |||||||
| Density d 4 20，g/cm 3 | 0.8890 | 0.8845 | 0.8841 | 0.8852 | 0.8843 | 0.8820 | 0.8861 |
| Sulphur, μ g/g | 450 | 167 | 270 | 271 | 160 | 143 | 162 |
| Desulfurization degree | 87.7 | 95.7 | 92.6 | 92.6 | 95.6 | 96.1 | 95.6 |
| Nitrogen, μ g/g | 112.0 | 141 | 45.0 | 53.2 | 23.1 | 13.3 | 16.1 |
| Denitrification percent | 86.8 | 98.2 | 94.7 | 93.7 | 97.3 | 98.4 | 98.1 |
| Cetane value | 34.6 | 37.9 | 39.1 | 38.5 | 39.9 | 40.2 | 34.2 |
| Cetane value amplification | 4.6 | 7.9 | 9.1 | 8.5 | 9.9 | 10.2 | 4.2 |
| Less than 180 ℃ of yields, w% | 1.3 | 1.6 | 2.1 | 1.9 | 2.6 | 2.9 | 1.1 |
Denitrification percent calculates by following formula: 100 * (raw material nitrogen content-product nitrogen content)/feed sulphur content
By table 5, table 6 as seen, the difference of molecular sieve in the catalyzer, its stability is different, adopts the catalyst stability of molecular sieve of the present invention better, and the proportioning of each component by regulating catalyst adds the stability that sial can improve catalyzer.
By above embodiment data as can be seen: catalyzer of the present invention not only has good desulfurization, nitrogen removal performance, and can obviously improve diesel cetane-number, therefore is suitable for handling poor ignition quality fuel especially, improves diesel quality comprehensively.
Claims (6)
1, a kind of catalyst for hydrocracking diesel oil, with aluminum oxide and Y zeolite is carrier, contain at least a group vib metal and at least a VIII family metal, it is characterized in that support of the catalyst consists of aluminum oxide 40～90w%, amorphous aluminum silicide 0～20w%, molecular sieve 5～40w%, Y zeolite pore volume 0.40～0.52ml/g wherein, specific surface 750～900m
2/ g, lattice constant 2.420～2.500nm, SiO
2/ Al
2O
3Than 7～15, the group vib metal oxide content is 10～30w% in the catalyzer, and VIII family metal oxide content is 2～15w%.
2,, it is characterized in that molecular sieve content is 10～30w% in the said carrier according to the catalyzer of claim 1.
3,, it is characterized in that said amorphous aluminum silicide SiO according to the catalyzer of claim 1
2/ Al
2O
3Weight ratio is 1: 2～2: 1.
4,, it is characterized in that amorphous aluminum silicide content is 10～20w% in the said carrier according to the catalyzer of claim 1.
5, according to the catalyzer of claim 1, it is characterized in that the group vib metal is selected from W, Mo, VIII family metal is selected from Ni, Co.
6, according to the catalyzer of claim 1, it is characterized in that the group vib metal is W, VIII family metal is Ni.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96120988A CN1049679C (en) | 1996-12-10 | 1996-12-10 | Catalyst for hydrogenation conversion of diesel |
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|---|---|---|---|
| CN96120988A CN1049679C (en) | 1996-12-10 | 1996-12-10 | Catalyst for hydrogenation conversion of diesel |
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| CN1184843A CN1184843A (en) | 1998-06-17 |
| CN1049679C true CN1049679C (en) | 2000-02-23 |
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| CN1102663A (en) * | 1993-08-30 | 1995-05-17 | 日本石油株式会社 | Process for hydrotreating heavy hydrocarbon oil |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448952C (en) * | 2005-04-29 | 2009-01-07 | 中国石油化工股份有限公司 | Hydrogenation cracking catalyst composition containing zeolite |
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