CN1458238A - Nobel metal hydrogen cracking catalyst and its preparing method - Google Patents
Nobel metal hydrogen cracking catalyst and its preparing method Download PDFInfo
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- CN1458238A CN1458238A CN 02109658 CN02109658A CN1458238A CN 1458238 A CN1458238 A CN 1458238A CN 02109658 CN02109658 CN 02109658 CN 02109658 A CN02109658 A CN 02109658A CN 1458238 A CN1458238 A CN 1458238A
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Abstract
The present invention discloses a kind of noble metal hydrogen cracking catalyst and its preparation process. The catalyst contains one carrier component, one modified Y-type zeolite, and one or two kinds of noble metal components. The catalyst features that the hydrogenating noble metal component is loaded onto the carrier component and that the modified superhydrophobic Y-type zeolite containing no hydrogenating component is deep treated to possess great specific surface area, great pore volume, proper acid distribution and high Si/Al ratio. The catalyst has high metal dispersivity, powerful carbon deposition resistance and certain sulfur resistance, and may be used in hydrogen cracking, hydrogenation, hydrogen modification, etc. of fraction oil with high selectivity to middle fraction oil.
Description
Technical field:
The present invention relates to a kind of noble metal catalyst that is used for hydrocarbon hydrocracking and preparation method thereof, especially for hydrocracking catalyst of producing intermediate oil and preparation method thereof.
Background technology:
At present, it is more and more heavier that each refinery of the world all is faced with raw material, quality problem worse and worse, and hydrocracking process has become one of important means of light materialization of heavy oil.Simultaneously, in the world wide middle distillate demand is constantly increased, thereby the exploitation of middle oil type hydrocracking catalyst is active day by day.
Hydrocracking catalyst is generally dual-function catalyst, and the cracking function is provided by acid carrier, and acid carrier can be that amorphous oxide is (as SiO
2-Al
2O
3), zeolite molecular sieve and heat-resistant inorganic oxide (as aluminum oxide) or their mixture.The component that hydrogenation-dehydrogenation functionality is provided can be that (Pd also can be that (Mo is W) with VIII family base metal (Co, oxide compound Ni) or sulfide for group vib Pt) to precious metal.Usually, non-precious metal catalyst is used for the aromatic hydrocarbons that the hydrocracking process products obtained therefrom can contain some amount, and in industrial application, wishes that aromaticity content is low as far as possible in rocket engine fuel and the diesel oil, and noble metal catalyst has shown its superiority in this respect.But traditional noble metal catalyst is higher because of its activity, and the gas production rate height has influenced product liquid and received, and the fragrant potential content of petroleum naphtha is low in the products obtained therefrom, can not be used as reformer feed.And the precious metal total amount that supports on the carrier is less, and hydrogenation component is supported on the acidic components in the catalyzer, and metal is difficult for being evenly distributed, thereby influences catalyzer use properties and stability.
United States Patent (USP) 6,174,430 disclose a kind of Nobel metal hydrogen cracking catalyst and preparation method thereof, this method for preparing catalyst is for carrying out ion-exchange with super-hydrophobic Y zeolite and the solution that contains precious metal earlier, obtain containing the Y zeolite of precious metal, again itself and oxide compound, water, a kind of peptizing agent, a kind of extrusion aid are mixed and pinch, extruded moulding, drying and roasting promptly get this catalyzer.The Y molecular sieve that contains 70m%-90m% in this catalyzer, SiO
2/ Al
2O
3Than being 4.8-＜6.0, lattice constant is 24.50-24.57nm, the Al of 10m%-30m%
2O
3, the precious metal of 0.5m%-1m% can be used for high yield petroleum naphtha and rocket engine fuel product, and wherein naphtha selective is about 32m%, and the rocket engine fuel selectivity is at 40m%.But as the molecular sieve content height of acidic components, acidity of catalyst is strong in this catalyzer, and cracking performance is strong, and handles depth as shallow, and the gained light-end products is more, and petroleum naphtha virtue potential content is low, and the intermediate oil selectivity is lower.
United States Patent (USP) 4175033 discloses a kind of Ni, Mo, Pt and has been supported on simultaneously and contains Y zeolite supported catalyst and preparation method.This catalyzer preparation earlier contains the Y zeolite carrier, floods Ni, Mo, Pt more respectively.The catalyzer of this patent preparation is because of containing precious metal and base metal simultaneously, and catalyzer has certain anti-sulphur, can be used for various hydrogenation techniques such as hydrocracking, hydrofining.Preparation of catalysts adopts prepares carrier earlier, and metal is introduced in the back.But the Preparation of catalysts method still adopts the traditional preparation process method in this patent, do not improve, it is less that existence supports bullion content, the problem that metal is difficult for being evenly distributed, hydrogenation center and cracking center on the catalyzer do not separate, thereby there is the not good enough problem of degree of uniformity equally in Metal Distribution, and distillate selectivity is lower in the middle of it.
Summary of the invention:
The object of the invention provides a kind of Nobel metal hydrogen cracking catalyst with oil in good metal dispersiveness and the fecund, the present invention also aims to provide a kind of preparation method of hydrocracking catalyst simultaneously, with acid sites and the hydrogenation center that further keeps apart catalyzer.
The present invention has adopted a kind of modified Y zeolite as the main acidic components of catalyzer, adopt the hydrogenation component precious metal is supported on the heat-resistant inorganic oxide simultaneously, the acid sites and the hydrogenation center that keep apart catalyzer again with the preparation method of Y zeolite moulding, further improve hydrogenation cracking activity and middle runnings oil type selectivity, can greatly preparing hihg-quality boat coal and wide cut diesel fuel.
Catalyzer of the present invention consists of (is benchmark with catalyst weight per-cent) modification super-hydrophobic Y zeolite 10m%-65m%, heat-resistant inorganic oxide 34.9m%-89.9m%, bullion content is 0.1m%-2.0m%, wherein the modification super-hydrophobic Y zeolite is characterised in that: unit cell parameters 2.420-2.450nm, degree of crystallinity 85-105%, SiO
2/ Al
2O
3Mol ratio 10-100, Na
2O weight content＜0.2m%.
The content of catalyzer the best of the present invention is Y zeolite 20m%-50m%, and heat-resistant inorganic oxide is preferably 50m%-80m%, and bullion content is preferably 0.3m%-1.2m%.
Specific surface area of catalyst 300-500m of the present invention
2/ g, pore volume 0.48-0.65ml/g.
Above-mentioned super-hydrophobic Y zeolite is at 25 ℃, p/p
0Under=0.1 condition, water adsorption amount＜5m%, specific surface area 700-900m
2/ g, pore volume 0.35-0.55ml/g, infrared acidity 0.2-2.0mmol/g.
The modification super-hydrophobic Y zeolite that catalyzer of the present invention is related, silica alumina ratio are preferably 10-90 (mol ratio), and unit cell parameters is preferably 2.425-2.435nm.
Compare with the Y zeolite of prior art for preparing, the related zeolite of catalyzer of the present invention has higher degree of crystallinity, specific surface, and form more weak acid center, its＞strong acid center of 450 ℃ of desorptions is generally less than 15%, and about 85% concentrates on the weak of 150-450 ℃ of desorption and middle strong acid center.Therefore, guarantee unlikely excessive fragmentation, but a certain amount of strong acid center has also guaranteed the lytic activity of catalyzer.Simultaneously, high-ratio surface and more secondary pore have also promoted the performance of hydrogenation activity, and satisfying has the middle oil type hydrocracking catalyst of medium lytic activity and high hydrogenation activity to the requirement of heavy hydrocarbon material cracked.
Heat-resistant inorganic oxide of the present invention can comprise active or inactive high-melting-point inorganic raw material, as clay, silicon oxide, aluminum oxide, sial, zirconium white, titanium oxide-magnesium oxide and their mixture, preferably aluminum oxide.
The precious metal that supports on heat-resistant inorganic oxide of the present invention is generally and is selected among Ru, Rh, Pd, Os, Ir, the Pt one or more, preferably one or both among Pd, the Pt.
Catalyst preparation process of the present invention is, heat-resistant inorganic oxide such as aluminum oxide contacted with the water-soluble salt solution that contains precious metal flood, after the drying, pinch extruded moulding with modified Y zeolite, peptizing agent, extrusion aid through mixing again, drying again, roasting (or hydrothermal treatment consists) promptly.
This preparation method will make as the Y zeolite of acidic components with as the precious metal of hydrogenation component and separate, and make catalyzer bring into play the hydrocracking synergistic effect more fully, obtain the purpose product.Simultaneously, also will further keep apart between the precious metal, avoid its gathering, optimized Metal Distribution, and the overflow hydrogen that comes out in hydrogenation center can suppress the second pyrolysis reaction, thereby reach the purpose of oil in the fecund.
Wherein used aluminum oxide specific surface area 400-500m
2/ g, pore volume 0.35-0.55ml/g; The dipping solution of used precious metal can be Ru, Rh, Pd, Os, Ir, Pt etc., the preferably water-soluble salt solution of Pd, Pt or its relative acid, and the pH value of solution value is 2.0-10.0, dipping time 6-24 hour,
The preparation method of modified Y zeolite of the present invention comprises: be that raw material carries out repeatedly the ammonium exchange with NaY, deviate from Na
+Behind the ion,, prepare modified Y zeolite of the present invention through twice hydrothermal treatment consists and acid treatment.
The related modifying super hydrophobicity Y zeolite preparation process of catalyzer of the present invention is as follows:
(1) be raw material with the NaY zeolite, ammonium exchange is washed afterwards, and wash temperature is 30-60 ℃, under 110 ± 10 ℃ of conditions dry 4-10 hour then.Until obtaining Na
2The Y zeolite of O＜0.2m%.Described NaY zeolite character is generally degree of crystallinity 95-105%, and unit cell parameters is 2.462-2.480nm.
(2) with the Y zeolite that obtains in the step (1) after filtration, washing, drying be placed in the water treatment stove, at self water vapour or feed water vapour, 450-750 ℃, the 0.05-0.5MPa pressure condition was handled 0.5-10 hour down.
(3) Y zeolite that obtains in the step (2) is placed contain H
+, NH
4 +Carry out acid treatment in the cationic aqueous solution, used ammonium salt can be NH
4NO
3, NH
4Cl, (NH
4)
2SO
4Deng, used acid can be HCl, HNO
3, H
2SO
4Deng, in the acid treatment process, the control pH value of solution should be 2.0-5.0, is preferably 2.0-4.0, and the acid treatment temperature is generally 60-100 ℃, treatment time 0.5-5 hour, handles after-filtration.
(4) step (3) is obtained sample and after washing, drying, carry out the secondary hydrothermal treatment consists, the same step of treatment condition (2).
(5) step (4) is obtained sample and carry out the quadratic acid processing, exchange liquid can be HCl, HNO
3, H
2SO
4Deng, strength of solution is 0.1-0.6mol/l, exchange is 0.5-2 hour under 50-100 ℃ of condition, and washing then, the same step of condition (1) under 100-140 ℃ of condition dry 4-8 hour afterwards, promptly gets modified Y zeolite of the present invention.
The precious metal that catalyzer of the present invention is related is incorporated on the heat-resistant inorganic oxide by impregnation method.Immersion condition is: under room temperature, the normal pressure, the precious metal steeping fluid is contacted with the ratio of inorganic oxide with 2: 1 (volume ratio), flooded 6-24 hour, magnetic agitation, the pH value is controlled at 2.0-10.0, and filter dried solution in dipping back dried in the shade through 8-24 hour, make the precious metal radial distribution more even, descended dry 6-48 hour in 110 ℃ ± 10 ℃ then.
Precious metal steeping fluid of the present invention can be Ru, Rh, Pd, Os, Ir, Pt etc., the preferably water-soluble salt solution of Pd, Pt or its relative acid.For example, the water soluble salt of Pd, Pt or its relative acid can be H
2PdCl
4, Pd (NO
3)
2, Pd (NH
3)
4Cl
2, Pd (NH
3)
4(NO
3)
2, H
2PtCl
4, Pt (NH
3)
4Cl
2, Pt (NH
3)
4(NO
3)
2, Pt (NO
3)
2Or the mixture of Pd, the corresponding salt of Pt.
The shape of catalyzer of the present invention can be sheet, spherical, cylinder bar and special-shaped bar (trifolium, Herba Galii Bungei), preferably cylinder bar and special-shaped bar (trifolium, Herba Galii Bungei).
Carrier and catalyzer drying conditions involved among the present invention are: 60 ℃ dry 2-3 hour, again in 110 ℃ ± 10 ℃ dry 6-48 hour down.
Carrier and catalyzer roasting condition involved among the present invention are: temperature 450-750 ℃, be preferably 500-650 ℃, and roasting time was generally 2-24 hour, was preferably 2-8 hour.
Catalyzer among the present invention after the moulding also can carry out hydrothermal treatment consists.The hydrothermal treatment consists condition is: pressure 0.05-0.5MPa, temperature 450-550 ℃.
Involved in the present invention to extrusion aid can be: sesbania powder, citric acid, oxalic acid, Mierocrystalline cellulose, starch, one or more of polymeric surface active agent etc.
Involved in the present invention to peptizing agent can be: Tai-Ace S 150, citric acid, nitric acid, acetic acid, oxalic acid etc.
Compared with prior art, catalyzer of the present invention has adopted high-specific surface area, and large pore volume and have that suitable acid distributes, the Y zeolite of high silica alumina ratio is made acidic components, and its moderate acidity has guaranteed that the reactive behavior of catalyzer and middle distillates oil selectivity and product liquid receive.Thereby, be used for the characteristics that oil type hydrocracking catalyst has high reactivity, high middle distillates oil selectivity.Simultaneously, owing to adopted precious metal supported on heat-resistant inorganic oxide, and prepare the method for catalyzer with the Y zeolite mixing moulding, to make acidity of catalyst center and hydrogenation center give full play to its effectiveness separately, the hydrogen that overflow at while hydrogenation center will suppress the generation of second pyrolysis on the acid sites, help improving middle distillates oil selectivity.And precious metal played protection, and further isolate, optimize the effect of precious metal dispersity, also finally help the performance of hydrogenation activity, be particularly suitable for middle oil type hydrocracking catalyst, satisfied catalyst activity and needs optionally.It is a kind of good Nobel metal hydrogen cracking catalyst.
The invention will be further described below by embodiment.
Example 1
1. the NaY zeolite 100g (degree of crystallinity 98%, unit cell parameters 2.462nm) that produces with Wenzhou catalyst plant is put in and is dissolved with 144g NH
4NO
3With 2.7ml concentrated nitric acid (dense HNO
3Proportion 1.4, concentration 65%) in the 1 premium on currency solution, be warming up to 90 ℃, stir 1.5 hours after-filtration, washing, drying.
2. the product that step 1 is obtained places in the hydrothermal treatment consists stove, handles 4 hours down for 600 ℃ in water partial pressure 0.3MPa, temperature.
3. product is put into the described 1 premium on currency solution of step 1, stirs 1 hour after-filtration down at 90 ℃, repeats once.
4. behind the repeating step 2,3, product was made modified zeolite of Y-type in 120 ℃ times dry 8 hours.
5. Germany is produced SB aluminum oxide powder (Al
2O
3Aluminium powder contents on dry basis 75%) 300g immerses the H of 550ml
2PdCl
4In the aqueous solution 24 hours, contain Pd 2.75g in the solution, magnetic agitation.Soak the dried solution of back filter, room temperature was dried in the shade 8 hours, and following dry 8 hours in 120 ℃.
6. the Germany that supports precious metal that obtains in resulting modified zeolite of Y-type and the step 5 in the step 4 being produced the SB aluminum oxide powder mixes, and adding 7ml concentrated nitric acid (65%) and an amount of water, adding 3g citric acid and 3g sesbania powder also mixes, on banded extruder, be extruded into Ф 1.5mm cylindrical bar, in 60 ℃ of dryings 3 hours, again in 120 ℃ dry 8 hours down, catalyst A is made in 550 ℃ of roastings 4 hours.
Example 2
1. the NaY zeolite 100g (degree of crystallinity 98%, unit cell parameters 2.462nm) that produces with Wenzhou catalyst plant is put in and is dissolved with 144g NH
4NO
3With 2.7ml concentrated nitric acid (dense HNO
3Proportion 1.4, concentration 65%) in the 1 premium on currency solution, be warming up to 70 ℃, stir 2 hours after-filtration, washing, drying.
2. the product that step 1 is obtained places in the hydrothermal treatment consists stove, handles 4 hours down for 650 ℃ in water partial pressure 0.2MPa, temperature.
3. product is put into the described 1 premium on currency solution of step 1, stirs 1 hour after-filtration down at 70 ℃, repeats once.
4. repeating step 2, carry out the secondary hydrothermal treatment consists after, product is put in the 1 premium on currency solution that is dissolved with 38ml concentrated nitric acid (1.4,65%), is warming up to 70 ℃, stirs 1 hour after-filtration, washing, drying, in 120 ℃ dry 8 hours down, make modified zeolite of Y-type.
5. Germany is produced SB aluminum oxide powder (Al
2O
3Aluminium powder contents on dry basis 75%) 200g immerses the H of 500ml
2PdCl
4In the aqueous solution 24 hours, contain Pd 2.5g in the solution, magnetic agitation.Soak the dried solution of back filter, room temperature was dried in the shade 8 hours, and following dry 8 hours in 120 ℃.
6. the Germany that supports precious metal that obtains in resulting modified zeolite of Y-type and the step 5 in the step 4 being produced the SB aluminum oxide powder mixes, and adding 4.5ml concentrated nitric acid (65%) and an amount of water, adding 2g citric acid and 2g sesbania powder also mixes, on banded extruder, be extruded into Ф 1.5mm cylindrical bar, in 60 ℃ of dryings 2 hours, again in 110 ℃ dry 8 hours down, catalyst B is made in 500 ℃ of roastings 6 hours.
Example 3
1. the NaY zeolite 100g (degree of crystallinity 98%, unit cell parameters 2.462nm) that produces with Wenzhou catalyst plant is put in and is dissolved with 144g NH
4NO
31 premium on currency solution in, be warming up to 80 ℃, stir 2 hours after-filtration, washing, drying.
2. the product that step 1 is obtained places in the hydrothermal treatment consists stove, handles 4 hours down for 600 ℃ in water partial pressure 0.15MPa, temperature.
3. product is put into the described 1 premium on currency solution of step 1, stirs 1 hour after-filtration down at 80 ℃, repeats once.
4. repeating step 2, carry out the secondary hydrothermal treatment consists after, product is put in the 1 premium on currency solution that is dissolved with 20ml concentrated nitric acid (1.4,65%), is warming up to 80 ℃, stirs 1 hour after-filtration, washing, drying, in 120 ℃ dry 8 hours down, make modified zeolite of Y-type.
5. Germany is produced SB aluminum oxide powder (Al
2O
3Aluminium powder contents on dry basis 75%) 200g immerses the Pd (NH of 500ml
3)
4Cl
2In the aqueous solution 24 hours, contain Pd 2.5g in the solution, magnetic agitation.Soak the dried solution of back filter, room temperature was dried in the shade 8 hours, and following dry 8 hours in 120 ℃.
6. the Germany that supports precious metal that obtains in resulting modified zeolite of Y-type and the step 5 in the step 4 being produced the SB aluminum oxide powder mixes, and adding 7.5ml concentrated nitric acid (65%) and an amount of water, adding 3g citric acid and 3g sesbania powder also mixes, on banded extruder, be extruded into Ф 1.5mm cylindrical bar, in 60 ℃ of dryings 2 hours, again in 120 ℃ dry 10 hours down, catalyzer C is made in 550 ℃ of roastings 4 hours.
Example 4
1. the NaY zeolite 100g (degree of crystallinity 98%, unit cell parameters 2.462nm) that produces with Wenzhou catalyst plant is put in and is dissolved with 144g NH
4NO
3With 2.7ml concentrated nitric acid (dense HNO
3Proportion 1.4, concentration 65%) in the 1 premium on currency solution, be warming up to 70 ℃, stir 2 hours after-filtration, washing, drying.
2. the product that step 1 is obtained places in the hydrothermal treatment consists stove, handles 4 hours down for 650 ℃ in water partial pressure 0.2MPa, temperature.
3. product is put into the described 1 premium on currency solution of step 1, stirs 1 hour after-filtration down at 70 ℃, repeats once.
4. behind the repeating step 2,3, product was made modified zeolite of Y-type in 120 ℃ times dry 8 hours.
5. Germany is produced SB aluminum oxide powder (Al
2O
3Aluminium powder contents on dry basis 75%) 245g immerses the Pd (NH of 450ml
3)
4Cl
2And H
2PtCl
4In the mixed aqueous solution 24 hours, contain Pd 1.8g in the solution, contain Pt 0.45g, magnetic agitation.Soak the dried solution of back filter, room temperature was dried in the shade 8 hours, and following dry 8 hours in 120 ℃.
6. the Germany that supports precious metal that obtains in resulting modified zeolite of Y-type and the step 5 in the step 4 being produced the SB aluminum oxide powder mixes, and adding 4.5ml concentrated nitric acid (65%) and an amount of water, adding 2.5g citric acid and 2.5g sesbania powder also mixes, on banded extruder, be extruded into Ф 1.5mm cylindrical bar, in 60 ℃ of dryings 3 hours, again in 120 ℃ dry 12 hours down, catalyzer D is made in 600 ℃ of roastings 4 hours.
Example 5
1. the NaY zeolite 100g (degree of crystallinity 98%, unit cell parameters 2.462nm) that produces with Wenzhou catalyst plant is put in and is dissolved with 144g NH
4NO
3With 2.7ml concentrated nitric acid (dense HNO
3Proportion 1.4, concentration 65%) in the 1 premium on currency solution, be warming up to 70 ℃, stir 2 hours after-filtration, washing, drying.
2. the product that step 1 is obtained places in the hydrothermal treatment consists stove, handles 4 hours down for 650 ℃ in water partial pressure 0.2MPa, temperature.
3. product is put into the described 1 premium on currency solution of step 1, stirs 1 hour after-filtration down at 70 ℃, repeats once.
4. behind the repeating step 2,3, product was made modified zeolite of Y-type in 120 ℃ times dry 8 hours.
5. Germany is produced SB aluminum oxide powder (Al
2O
3Aluminium powder contents on dry basis 75%) 245g immerses the Pd (NH of 450ml
3)
4Cl
2In the aqueous solution 24 hours, contain Pd 2.25g in the solution, magnetic agitation.Soak the dried solution of back filter, room temperature was dried in the shade 8 hours, and following dry 8 hours in 120 ℃.
6. the Germany that supports precious metal that obtains in resulting modified zeolite of Y-type and the step 5 in the step 4 being produced the SB aluminum oxide powder mixes, and adding 4.5ml concentrated nitric acid (65%) and an amount of water, adding 2.5g citric acid and 2.5g sesbania powder also mixes, on banded extruder, be extruded into Ф 1.5mm cylindrical bar, room temperature was dried in the shade 8 hours, placed the hydrothermal treatment consists stove to carry out hydrothermal treatment consists afterwards, and temperature is 500 ℃, pressure is 0.3MPa, makes catalyzer E.
Listed in the table 1 catalyst A-E of the present invention and used molecular sieve thereof physico-chemical property
Table 1 catalyst A-E of the present invention and used molecular sieve thereof physico-chemical property
| Catalyzer | ?A | ?B | ?C | ?D | ?E |
| Molecular sieve character | |||||
| SiO 2/Al 2O 3 | ?31.05 | ?63.3 | ?12.6 | ?31.05 | ?64.2 |
| Degree of crystallinity, % | ?98 | ?102 | ?98 | ?97 | ?101 |
| ?a 0，nm | ?2.432 | ?2.430 | ?2.433 | ?2.432 | ?2.430 |
| Specific surface area, m 2/g | ?800 | ?830 | ?780 | ?800 | ?830 |
| Pore volume, ml/g | ?0.499 | ?0.527 | ?0.510 | ?0.497 | ?0.527 |
| ?Na 2O，m％ | ?0.2 | ?0.2 | ?0.2 | ?0.2 | ?0.2 |
| ?NH 3-TPD | |||||
| ?150-250℃ | ?35.0 | ?48.4 | ?42.6 | ?35.2 | ?39.1 |
| ?250-400℃ | ?65.0 | ?43.5 | ?44.8 | ?63.5 | ?57.7 |
| ?400℃ | ?0.0 | ?8.1 | ?3.3 | ?1.2 | ?1.5 |
| ?＞450℃ | ?0.0 | ?0.0 | ?9.3 | ?0.0 | ?1.7 |
| Total acid | ?0.12 | ?0.37 | ?0.38 | ?0.21 | ?0.19 |
| The meleic acid amount, mmol/g | ?0.319 | ?0.258 | ?0.400 | ?0.319 | ?0.258 |
| Catalyzer is formed | |||||
| Molecular sieve, m% | ?17.4 | ?25.5 | ?40.2 | ?22.2 | ?22.4 |
| Aluminum oxide, m% | ?81.68 | ?73.65 | ?59.03 | ?76.94 | ?76.8 |
| ?Pd，m％ | ?0.81 | ?0.73 | ?0.69 | ?0.72 | ?0.78 |
| ?Pt，m％ | ?- | ?- | ?- | ?0.12 | ?- |
| Specific surface area, m 2/g | ?345 | ?340 | ?306 | ?353 | ?327 |
| Pore volume, ml/g | ?0.582 | ?0.596 | ?0.570 | ?0.610 | ?0.575 |
Example 6
High reactivity and high middle distillates oil selectivity in order to further specify catalyzer of the present invention adopt catalyzer of the present invention, are raw material with the hydrocracking tail oil, carry out the hydrogenation cracking activity evaluation of distillate.The evaluation of catalyzer is carried out on the 100ml hydrogenation unit, measures the 50ml catalyzer and the reactor of packing into volume 20-30 order quartz sand mixing, carries out hydrogen reduction earlier, and then carries out the hydrogenation cracking activity evaluation.Stock oil character sees Table 2, and evaluation result sees Table 3.
Table 2 stock oil character
| Physical index | Stock oil |
| Density, g/cm 3(20℃) | ????0.8426 |
| Boiling range, ℃ | |
| ????10％ | ????372.2 |
| ????50％ | ????415.1 |
| ????90％ | ????495.9 |
| ????EBP | ????554.6 |
| Viscosity (50 ℃), mm 2/s | ????13.81 |
| Viscosity (100 ℃), mm 2/s | ????4.294 |
| Flash-point, ℃ (opening) | ????210 |
| Acid number, MgKOH/100ml | ????0.03 |
| Refractive index, n D 70 | ????1.4476 |
| ????S，μg/g | ????10 |
| ????N，μg/g | ????1.0 |
| ????C/H | ????84.85/13.81 |
Table 3 hydrogenation cracking activity evaluation result
| The catalyzer numbering | ????A | ????B | ????C | ????D | ????E |
| Reaction conditions | |||||
| The hydrogen dividing potential drop, MPa | ????14.7 | ????14.7 | ????14.7 | ????14.7 | ????14.7 |
| Volume space velocity, h -1 | ????2.0 | ????2.0 | ????2.0 | ????2.0 | ????2.0 |
| Hydrogen-oil ratio (v) | ????1000 | ????1000 | ????1000 | ????1000 | ????1000 |
| Temperature of reaction, ℃ | ????332 | ????330 | ????327 | ????332 | ????328 |
| Product selectivity, w% | |||||
| ＜82℃ | ????5.9 | ????5.1 | ????4.4 | ????5.5 | ????6.3 |
| 82～132℃ | ????9.8 | ????10.5 | ????9.6 | ????10.2 | ????10.9 |
| 132～282℃ | ????32.2 | ????34.8 | ????32.5 | ????34.7 | ????33.6 |
| 282～370℃ | ????20.3 | ????16.6 | ????19.5 | ????18.8 | ????18.3 |
| ＞370℃ | ????30.3 | ????31.3 | ????33.0 | ????29.8 | ????29.1 |
| Transformation efficiency, w% | ????68.2 | ????67.0 | ????66.0 | ????69.2 | ????69.1 |
| Middle distillates oil selectivity, w% | ????76.9 | ????76.7 | ????78.8 | ????77.3 | ????75.1 |
| Liquid is received, w% | ????98.5 | ????98.3 | ????99.0 | ????99.0 | ????98.2 |
By data in the table 3 as can be seen, this catalyzer has higher hydrogenation cracking activity, reaching＞when 370 ℃ of per pass conversion were 66-69%, the product middle distillates oil selectivity was still very high, and all more than 75%, and temperature of reaction is not higher than 350 ℃, and C
4Following gas-selectively is low, and liquid is received high, is the hydrocracking catalyst of oil in a kind of good fecund.
Claims (10)
1, a kind of Nobel metal hydrogen cracking catalyst, it is characterized in that catalyzer consists of modification super-hydrophobic Y zeolite 10m%-65m%, heat-resistant inorganic oxide 34.9m%-89.9m%, bullion content is 0.1m%-2.0m%, wherein the modification super-hydrophobic Y zeolite is characterised in that: unit cell parameters 2.420-2.450nm, degree of crystallinity 85-105%, SiO
2/ Al
2O
3Mol ratio 10-100, Na
2O weight content＜0.2m%.
2,, it is characterized in that catalyzer consists of modification super-hydrophobic Y zeolite 20m%-50m%, heat-resistant inorganic oxide 50m%-80m%, bullion content 0.3m%-1.2m% according to the described hydrocracking catalyst of claim 1.
3, according to the described hydrocracking catalyst of claim 1, it is characterized in that specific surface area of catalyst 300-500m
2/ g, pore volume 0.48-0.65ml/g.
4,, it is characterized in that described super-hydrophobic Y zeolite at 25 ℃, p/p according to the described hydrocracking catalyst of claim 1
0Under=0.1 condition, water adsorption amount＜5m%, specific surface area 700-900m
2/ g, pore volume 0.35-0.55ml/g, infrared acidity 0.2-2.0mmol/g.
5, according to the described hydrocracking catalyst of claim 1, it is characterized in that described super-hydrophobic Y zeolite silica alumina ratio is 10-90, unit cell parameters is 2.425-2.435nm.
6, according to the described hydrocracking catalyst of claim 1, it is characterized in that in the wherein said super-hydrophobic Y zeolite＞strong acid center of 450 ℃ of desorptions smaller or equal to 15%, 85% acid site concentrate on the weak of 150-450 ℃ of desorption and in strong acid center.
7,, it is characterized in that described precious metal is to be selected among Ru, Rh, Pd, Os, Ir, the Pt one or more according to the described hydrocracking catalyst of claim 1.
8,, it is characterized in that described precious metal is one or both among Pd, the Pt according to the described hydrocracking catalyst of claim 1.
9, the described Preparation of catalysts method of a kind of claim 1 is characterized in that preparation process is:
Heat-resistant inorganic oxide contacted with the water-soluble salt solution that contains precious metal flood, after the drying, pinch through mixing with modified Y zeolite, peptizing agent, extrusion aid again, extruded moulding, drying again, roasting or hydrothermal treatment consists are promptly.
10, according to the described preparation method of claim 9, wherein involved carrier and catalyzer drying conditions are: 60 ℃ dry 2-3 hour, again in 110 ℃ ± 10 ℃ dry 6-48 hour down; Said roasting condition is: temperature 450-750 ℃, roasting time was generally 2-24 hour.
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| CN 02109658 CN1205317C (en) | 2002-05-15 | 2002-05-15 | Nobel metal hydrogen cracking catalyst and its preparing method |
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| CN 02109658 CN1205317C (en) | 2002-05-15 | 2002-05-15 | Nobel metal hydrogen cracking catalyst and its preparing method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100340336C (en) * | 2004-10-29 | 2007-10-03 | 中国石油化工股份有限公司 | Aluminosilicate containing molecular sieve catalyst, its preparation method and application |
| CN100360221C (en) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | Alumina supporter containing modified gamma zeolite and its preparation method |
| CN100360235C (en) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | Alumina supporter containing composite zeolite and its preparation method |
| CN109954511A (en) * | 2017-12-22 | 2019-07-02 | 中国石油化工股份有限公司 | A kind of reduction-state Nobel metal hydrogen cracking catalyst |
-
2002
- 2002-05-15 CN CN 02109658 patent/CN1205317C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100340336C (en) * | 2004-10-29 | 2007-10-03 | 中国石油化工股份有限公司 | Aluminosilicate containing molecular sieve catalyst, its preparation method and application |
| CN100360221C (en) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | Alumina supporter containing modified gamma zeolite and its preparation method |
| CN100360235C (en) * | 2004-10-29 | 2008-01-09 | 中国石油化工股份有限公司 | Alumina supporter containing composite zeolite and its preparation method |
| CN109954511A (en) * | 2017-12-22 | 2019-07-02 | 中国石油化工股份有限公司 | A kind of reduction-state Nobel metal hydrogen cracking catalyst |
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| Publication number | Publication date |
|---|---|
| CN1205317C (en) | 2005-06-08 |
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