CN1219030C - Method for hydrogen cracking - Google Patents
Method for hydrogen cracking Download PDFInfo
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- CN1219030C CN1219030C CN 02109657 CN02109657A CN1219030C CN 1219030 C CN1219030 C CN 1219030C CN 02109657 CN02109657 CN 02109657 CN 02109657 A CN02109657 A CN 02109657A CN 1219030 C CN1219030 C CN 1219030C
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Abstract
The present invention provides a hydrocracking method for simultaneously improving medium oil selectivity and product quality. Through the delaminated loading of a catalyst containing a Y-type molecular sieve and a catalyst containing a beta-type molecular sieve in a reactor, the catalyst containing a beta-type molecular sieve is loaded into the upper part of the reactor, the catalyst containing a Y-type molecular sieve is loaded into the lower part of the reactor, or the catalyst containing a Y-type molecular sieve is loaded into the upper part of the reactor, and the catalyst containing a beta-type molecular sieve is loaded into the lower part of the reactor to fully exert respective characteristics of the two different types of molecular sieve catalysts. The quality of a target product is improved while the medium oil selectivity of the catalysts is improved.
Description
1, technical field
The present invention relates to a kind of method for hydrogen cracking, particularly can improve the method for hydrocracking selectivity and quality product simultaneously.
2, background technology
Along with fraction oil demand between city's field alignment constantly increases, need the refinery to produce more intermediate oil.Simultaneously, the new millennium has also produced the notion of clean fuel to the concern of environment, and new oil fuel standard has proposed stricter requirement to indexs such as the sulphur of vapour, diesel oil and aromatic hydrocarbons.Obviously, time processing means and FCC technology can not satisfy the index request of market to clean fuel.Hydrocracking process is not only the secondary processing means of heavy feed stock lighting, obtains a kind of important means of high-quality rocket engine fuel and clean diesel especially from inferior raw material.World's hydrocracking nineties ability is in continuous increase, and new capacity is mainly used in middle oil production.The market requirement has also promoted hydrocracking technology in recent years high speed development.Hydrocracking catalyst is one of key of hydrocracking technology, and therefore, the middle oil type especially exploitation of medium oil type hydrocracking catalyst also becomes increasingly active.
What at present, be used for that maximum produces that the cracking component of the hydrocracking catalyst of intermediate oil extensively adopts is Y zeolite, beta molecular sieve or compound use Y, beta molecular sieve in a catalyzer.The characteristics of the catalyzer for preparing for the cracking component with the Y zeolite are good product qualities, but middle distillates oil selectivity does not contain beta molecular sieve catalyzer height.With the beta molecular sieve is the catalyzer middle distillates oil selectivity height of cracking component preparation, but its heavy naphtha virtue is latent low, tail oil BMCI value is high, and it is poor that quality product contains the Y zeolite catalyzer.Although middle distillates oil selectivity can be brought up to the level that contains the beta molecular sieve catalyzer after adopting composite Y, beta molecular sieve, the quality of heavy naphtha is also improved greatly, and the character of tail oil is improved less.
USP5279726 has introduced a kind of catalyzer that contains composite Y, beta molecular sieve, and wherein the lattice constant of Y zeolite is 24.46-24.62A, and total silica alumina ratio is 5.1-6.0, content 15-50w%.The silica alumina ratio of beta molecular sieve is 10-100, preferably 20-30.The hydrogenation metal component is oxide compound or the sulfide of Ni, the Co of the oxide compound of Mo, W of VIB or sulfide and VIII.β and the Y zeolite weight ratio in catalyzer is 2: 1-1: 2.Remove and also contain the above aluminum oxide of 10w% in the said components catalyzer.This invention catalyzer is compared with not containing wherein a kind of catalyzer of molecular sieve no matter in one section and two sections flow processs, and activity significantly improves, and yield of gasoline obviously increases.
USP4612108 has introduced a kind of catalyzer that contains beta molecular sieve, and this catalyzer is mainly used in the Hydrodewaxing of petroleum fractions.The content of beta molecular sieve in catalyzer is 5-50w% along with the direction of reactor stream increases gradually at the first bed beta molecular sieve content, and in the end bed beta molecular sieve content is 50-90w%.The silica alumina ratio of beta molecular sieve was at least 30: 1.Layering filling by catalyzer has improved 415 ℃
+The dewaxing rate of cut.
3, summary of the invention
Purpose of the present invention is exactly by the layering filling in reactor of catalyzer that contains Y zeolite and the catalyzer that contains beta molecular sieve, to give full play to the characteristics separately of two kinds of dissimilar molecular sieve catalysts, when improving the catalyzer middle distillates oil selectivity, improve the quality of purpose product.
The method applied in the present invention is, at single hop once in the cracking case by, one-stage serial or two sections flow processs, adopt the classification filling scheme of catalyzer: the top of reactor filling 10-90v% contain the Y zeolite catalyzer, contain the beta molecular sieve catalyzer at the bottom of reactor filling 10-90v%.Perhaps, the top of reactor filling 10-90v% contain the beta molecular sieve catalyzer, contain the Y zeolite catalyzer at the bottom of reactor filling 10-90v%.
The Y zeolite that contains in the Y zeolite catalyzer can adopt hydrothermal treatment consists method, chemical method, hydro-thermal to prepare with methods such as acid treatment combine.The content of Y zeolite in catalyzer is 5-60w%.Silica alumina ratio is 4-35, and lattice constant is 24.20-24.55A, and relative crystallinity is 75-100%, Na
2O content 0.005-0.2w%.Except that Y zeolite, can contain components such as aluminum oxide, amorphous silicon aluminium in the catalyst base, its content is 5-79w%, in addition, catalyzer also contains VIB and the VIII family element of 16-35w% (in oxide compound), as among W, Mo, Ni or the Co one or more.
The beta molecular sieve that contains in the beta molecular sieve catalyzer can adopt hydrothermal treatment consists method, hydrothermal treatment consists and the production of acid treatment combined techniques.The content of beta molecular sieve in catalyzer is 5-60w%.The beta molecular sieve silica alumina ratio is 10-200, and relative crystallinity is 80-150.Except that molecular sieve, can contain components such as aluminum oxide, amorphous silicon aluminium in the catalyst base, its content is 5-79w%, in addition, catalyzer also contains VIB and the VIII family element of 16-35w% (in oxide compound), as among W, Mo, Ni or the Co one or more.
Contain Y and the beta molecular sieve catalyzer can adopt coprecipitation method, kneading method, immersion process for preparing.
Hydrocracking can be handled VGO, CGO, deasphalted oil, LCO or their mixture.The processing condition of hydrocracking reaction are: reaction pressure 4.0-16.0MPa, air speed 0.1-10h
-1, hydrogen to oil volume ratio 300: 1-2000: 1, temperature of reaction 280-450 ℃.
Hydrocracking process can adopt two sections flow processs, single hop list agent flow process, hydrofining-hydrocracking one-stage serial flow process.Can adopt once technology by, part circulation or recycle to extinction.
By adopting this patent layering loading catalyst, contain the catalyzer ratio of Y zeolite with independent employing, under same process condition and identical stock oil, middle distillates oil selectivity improves 2-8m%.Contain the catalyzer ratio of beta molecular sieve with independent employing, under same process condition and identical stock oil, the heavy naphtha virtue is dived and is improved 2-10m%, 2-15 percentage point of tail oil BMCI value decline.
4, embodiment
Characteristics below by specific examples explanation this patent.
Embodiment 1
166 gram USY molecular sieves (hydrothermal treatment consists method, silica alumina ratio 5.07, lattice constant 24.48A, degree of crystallinity 76%, butt 70%), 133 are restrained by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 32.4 gram molybdenum oxides, 44 gram nickelous nitrates are put into rolling machine, grind to can squeezing paste, and extrusion, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-1.
Embodiment 2
107 gram US-SSY molecular sieves (behind the ammonium silicofluoride aqueous solution processing ammonium sodium Y molecular sieve, hydrothermal treatment consists, silica alumina ratio 10.6, lattice constant 24.37A, degree of crystallinity 90%, butt 75%), 133 are restrained by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 62.8 gram macroporous aluminium oxide powder (pore volume 0.92ml/g, specific surface area 270m
2/ g, butt 70%) put into rolling machine, grind to can squeezing paste, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 3 hours, with ammonium metawolframate, nickel nitrate aqueous solution dipping, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-2.Catalyzer contains WO
322.0w%, NiO 6.0w%.
Embodiment 3
54.8 gram NTY molecular sieves (hydrothermal treatment consists and the preparation of acid treatment combined techniques, silica alumina ratio 12.53, lattice constant 24.38A, degree of crystallinity 96%, butt 73%), 133 are restrained by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 42.8 gram macroporous aluminium oxide powder (pore volume 0.92ml/g, specific surface area 270m
2/ g, butt 70%), 45 gram amorphous silicon aluminiums put into rolling machine, grind to squeezing paste, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 3 hours are with ammonium metawolframate, nickel nitrate aqueous solution dipping, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-3.Catalyzer contains WO
324.5w%, NiO 6.5w%.
Embodiment 4
107 gram beta-molecular sieves (hydrothermal treatment consists and the preparation of acid treatment combined techniques, silica alumina ratio 70, butt 75%), 133 are restrained by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 42.8 gram macroporous aluminium oxide powder (pore volume 0.92ml/g, specific surface area 270m
2/ g, butt 70%) put into rolling machine, grind to can squeezing paste, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 3 hours, with ammonium metawolframate, nickel nitrate aqueous solution dipping, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-4.Catalyzer contains WO
323.0w%, NiO 5.5w%.
Embodiment 5
53.3 gram beta-molecular sieves (hydrothermal treatment consists and the preparation of acid treatment combined techniques, silica alumina ratio 26.5, butt 75%), 133 are restrained by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 42.8 gram macroporous aluminium oxide powder (pore volume 0.92ml/g, specific surface area 270m
2/ g, butt 70%) put into rolling machine, grind to can squeezing paste, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 3 hours, with ammonium metawolframate, nickel nitrate aqueous solution dipping, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-5.Catalyzer contains WO
324.3w%, NiO 5.3w%.
Comparative example-1
With 53.3 gram beta-molecular sieves (hydrothermal treatment consists and the preparation of acid treatment combined techniques, silica alumina ratio 26.5, butt 75%), 54.8 gram USSSY molecular sieve (lattice constant 24.37A, degree of crystallinity 90%, butt 75%), 133 grams are by SB powder (pore volume 0.46ml/g, specific surface area 260m
2/ g, butt 30%) tackiness agent of preparation, 42.8 gram macroporous aluminium oxide powder (pore volume 0.92ml/g, specific surface area 270m
2/ g, butt 70%) put into rolling machine, grind to can squeezing paste, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 3 hours, with ammonium metawolframate, nickel nitrate aqueous solution dipping, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 3 hours make catalyzer C-6.Catalyzer contains WO
325.0w%, NiO 5.1w%.
Comparative example-2
With Iranian VGO is raw material (character sees Table 1), at hydrogen dividing potential drop 14.7MPa, hydrogen to oil volume ratio 1500: 1, volume space velocity 1.5h
-1Under the situation, C-1～C-5 catalyzer is estimated.The results are shown in following table 2.
Embodiment 6
Load C-5, C-4 and C-2 respectively on cracking case top, bottom filling C-3, C-1 and C-4, the filling ratio was respectively 1: 1,5: 1 and 1: 7.Under the condition identical, estimate with comparative example-1.The results are shown in Table 2.As can be seen from Table 2, the catalyzer of layering filling is when keeping higher middle distillates oil selectivity, and product property also obviously improves.
The Iranian VGO character of table 1
| Density | 0.9028 |
| Boiling range, ℃ | 277-551 |
| Sulphur, m% | 1.54 |
| Nitrogen, ppm | 1440 |
| Condensation point, ℃ | 34 |
| C/H，m％ | 85.4/11.5 |
Table 2 evaluation result
| Catalyzer | Temperature of reaction *, ℃ | Middle distillates oil selectivity **，m％ | The heavy naphtha virtue is dived m% | Tail oil BMCI value |
| C-1 | 371 | 70.6 | 66.0 | 10.9 |
| C-2 | 370 | 72.7 | 65.8 | 9.9 |
| C-3 | 383 | 80.3 | 65.7 | 11.2 |
| C-4 | 374 | 81.9 | 60.5 | 17.7 |
| C-5 | 378 | 82.2 | 61.5 | 16.6 |
| C-5/C-3 | 377 | 83.0 | 65.9 | 11.0 |
| C-4/C-1 | 369 | 82.5 | 66.1 | 10.6 |
| C-2/C-4 | 366 | 82.0 | 64.5 | 12.3 |
*Temperature of reaction when controlling＜350 ℃ of per pass conversion 70m%
*Middle distillates oil selectivity=282～350 ℃ cut yield/(100-〉350 ℃ cut yield)
Claims (9)
1, a kind of method for hydrogen cracking is characterized in that adopting the classification filling scheme of catalyzer: the top of reactor filling 10-90v% contain the Y zeolite catalyzer, contain the beta molecular sieve catalyzer at the bottom of reactor filling 10-90v%.
2, in accordance with the method for claim 1, hydrothermal treatment consists method, chemical method or hydro-thermal and acid treatment bonded method are adopted in the preparation that it is characterized in that said Y zeolite.
3, in accordance with the method for claim 1, it is characterized in that the content of said Y zeolite in catalyzer is 5-60w%.
4, in accordance with the method for claim 1, the silica alumina ratio that it is characterized in that said Y zeolite is 4-35, and lattice constant is 24.20-24.55A, and relative crystallinity is 75-100%, Na
2O content 0.005-0.2w%.
5, in accordance with the method for claim 1, it is characterized in that containing aluminum oxide and/or amorphous silicon aluminium component in the Y zeolite catalyzer said containing, content is 5-79w%.
6, in accordance with the method for claim 1, it is characterized in that the content of said beta molecular sieve in catalyzer is 5-60w%.
7, in accordance with the method for claim 1, it is characterized in that said beta molecular sieve silica alumina ratio is 10-200, relative crystallinity is 80-150.
8, in accordance with the method for claim 1, it is characterized in that the handled raw material of this method is VGO, CGO, deasphalted oil, LCO or their mixture.
9, in accordance with the method for claim 1: the processing condition that it is characterized in that hydrocracking reaction are: reaction pressure 4.0-16.0MPa, air speed 0.1-10h
-1, hydrogen to oil volume ratio 300: 1-2000: 1, temperature of reaction 280-450 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02109657 CN1219030C (en) | 2002-05-15 | 2002-05-15 | Method for hydrogen cracking |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02109657 CN1219030C (en) | 2002-05-15 | 2002-05-15 | Method for hydrogen cracking |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200510078764 Division CN1290978C (en) | 2002-05-15 | 2002-05-15 | Hydrocracking process |
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| Publication Number | Publication Date |
|---|---|
| CN1458237A CN1458237A (en) | 2003-11-26 |
| CN1219030C true CN1219030C (en) | 2005-09-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 02109657 Expired - Lifetime CN1219030C (en) | 2002-05-15 | 2002-05-15 | Method for hydrogen cracking |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100569921C (en) * | 2006-06-16 | 2009-12-16 | 中国石油化工股份有限公司 | A kind of single-stage hydrocracking process |
| CN101343560B (en) * | 2007-07-09 | 2011-12-21 | 中国石油化工股份有限公司 | Process for preparing hydrocracking catalyst of high activity |
| CN101343559B (en) * | 2007-07-09 | 2011-12-21 | 中国石油化工股份有限公司 | Hydrocracking catalyst and preparation thereof |
| CN106669861B (en) * | 2015-11-11 | 2019-03-19 | 中国石油化工股份有限公司 | Hydrocracking catalyst grading method and catalytic diesel oil hydroconversion process |
| CN114160191B (en) * | 2021-12-02 | 2023-07-14 | 万华化学集团股份有限公司 | Catalytic cracking catalyst and preparation method and application thereof |
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