CN103769220B - A kind of preparation method of catalyst for hydrogenation of fraction oil - Google Patents
A kind of preparation method of catalyst for hydrogenation of fraction oil Download PDFInfo
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Abstract
The invention discloses a kind of preparation method of catalyst for hydrogenation of fraction oil.The method adopts substep to spray method, and first load in catalyst carrier by least one in group vib metal, Organic Alcohol and organic sugar, and then group VIII metal and organic acid are loaded to catalyst carrier, drying prepares hydrotreating catalyst.The method organic compound consumption is few, and dipping solution viscosity is little, prepares simple, and obtained hydrotreating catalyst activity is high, good stability.Hydrotreating catalyst of the present invention is particularly useful in diesel hydrogenation for removal sulphur technique.
Description
Technical field
The present invention relates to a kind of preparation method of catalyst for hydrogenation of fraction oil, especially for the preparation method of the hydrotreating catalyst of deep hydrodesulfurizationof of diesel oil.
Background technology
Along with the heaviness of crude oil, in poor quality and sulfur crude processing amount are in the trend risen year by year, the impurity contents such as the sulphur in diesel raw material, nitrogen and colloid are increased.On the other hand, increasingly strict along with environmental regulation, more and more harsher to the requirement of diesel product quality, especially more strict to the requirement of the sulfur content in diesel oil, Cetane number and polycyclic aromatic hydrocarbon content, secondary processing diesel oil has to pass through the diesel quality index request that deep hydrofinishing could meet high standard.
Along with the low sulfuration of diesel oil, Hydrofining Technology seems more and more important.Although reactor volume can be increased, increases recycle hydrogen de H by improving reaction temperature, reduction reaction velocity, reconstruction or new device
2s device, reduce cut cut point and adopt more the mode such as high activated catalyst to improve desulfurization depth, but improve reaction temperature can increase energy consumption and shorten catalyst service life, reduce reaction velocity and can reduce treating capacity, reconstruction or new device can increase plant investment and catalyst amount, by contrast, most economical and easy method selects optimal high activity deep hydrodesulfurizationof of diesel oil catalyst according to device working condition.
CN1938087B, US7737071B2, EP1733787A1 describe a kind of preparation method of hydrogenation catalyst, comprise: with comprising the compound of group vib metal, phosphorus containing components, the compound of group VIII metal and organic acid solution impregnating carrier, then under 200 DEG C or lower temperature, carry out drying, obtain catalyst.In the catalyst, coming from organic acid C content is 2% ~ 14%.
EP0870003B2 describes a kind of method preparing hydrogenation catalyst, comprise: with the solution impregnating carrier comprising the compound of group vib metal, the compound of group VIII metal and Organic Alcohol and/or sugar, then under 200 DEG C or lower temperature, carry out drying, obtain catalyst.In the catalyst, the C content coming from Organic Alcohol and/or sugar is 2% ~ 10%.
The defect of above-mentioned patent is that in catalyst, organic compound content is too high, because dipping solution viscosity causes greatly catalyst preparing difficulty to increase in preparation process, preparation time is long, but also can affect active metal distribution etc. on a catalyst.Because organic compound content is high, solution viscosity is large, and the reasons such as skewness, can make catalyst in high temperature vulcanized process, produce excessive sulfurate activity and pile up neatly layer mutually, affect the decentralization of active metal, and then affect the activity of catalyst.In addition, adopt organic acid separately in above-mentioned patented method, or adopt separately Organic Alcohol or/and sugar, though can improve the activity of catalyst so to a certain extent, the activity of catalyst need further raising.
Summary of the invention
For the deficiencies in the prior art part, the invention provides the preparation method of the high catalyst for hydrogenation of fraction oil of a kind of activity.Dipping solution viscosity prepared by the method is little, prepares simple.
The preparation method of hydrotreating catalyst of the present invention, described catalyst take aluminium oxide as carrier, with at least one group vib metal and at least one group VIII metal for hydrogenation active metals, containing organic compound in catalyst, organic compound comes from organic acid and is selected from least one in Organic Alcohol and organic sugar, this catalyst adopts infusion process load regulation group vib metal on the alumina support, group VIII metal and organic compound, the addition of organic compound accounts for the 1.0wt% ~ 1.8wt% of hydrotreating catalyst weight in C, be preferably 1.2wt% ~ 1.6wt%, process comprises:
(1) dipping solution I and dipping solution II is prepared respectively, wherein dipping solution I be by containing at least one in group vib metal and Organic Alcohol and organic sugar and water formulated, dipping solution II is by formulated containing group VIII metallic compound and organic acid, water, wherein organic acid addition is in the mol ratio of C and group VIII metal for 0.01 ~ 0.70, is selected from least one in Organic Alcohol and organic sugar in the mol ratio of C and group vib metal for 0.01 ~ 0.40;
(2) first use dipping solution I oxide impregnation alumina supporter, at the temperature of less than 200 DEG C after drying, then flood with dipping solution II, dry at the temperature of less than 200 DEG C, obtain hydrotreating catalyst.
Described hydrotreating catalyst, with at least one group vib metal and at least one group VIII metal for hydrogenation active metals, with the weight of catalyst for benchmark, hydrogenation active metals for 14% ~ 50%, is preferably 15% ~ 40% with the weight content of oxide basis.In described hydrotreating catalyst, group vib metal is preferably Mo and/or W, and group VIII metal is preferably Ni and/or Co.In described hydrotreating catalyst, group VIII metal/(group vib metal+group VIII metal) is with the weight ratio of the weight ratio of oxide basis (being abbreviated as VIII/(VIB+VIII in the present invention)) be 0.30 ~ 0.55.
It is at least one in the binary acid of 2 ~ 10 that described organic acid is selected from carbon number, is preferably one or more in citric acid, citric anhydride, isocitric acid, malic acid, tartaric acid, oxalic acid, butanedioic acid, glutaric acid, adipic acid, benzoic acid, phthalandione, isophathalic acid, salicylic acid, malonic acid; Described Organic Alcohol be selected from carbon number be 3 ~ 10 fatty alcohol and dihydroxylic alcohols in one or more, be preferably fatty alcohol, ethylene glycol, propyleneglycoles, glycerine, three methylol ethane, three methylol propane, divinyl ethylene glycol, two propyleneglycoles, trimethylene ethylene glycol, trietbhlene glycol, tributylene glycol, four ethylene glycols, tetrapropylene ethylene glycol, polyethylene glycol, divinyl Propylene Glycol, divinyl ethohexadiol, divinyl propyl glycol, one or more in divinyl butyl glycol; It is the monose of 3 ~ 10, at least one in disaccharides and polysaccharide that described organic sugar is selected from carbon number.
Can also contain auxiliary agent phosphorus in described catalyst, phosphorus weight content is in the catalyst 0.01% ~ 2.5%.
The character of hydrotreating catalyst of the present invention is as follows: pore volume is 0.3 ~ 1.3ml/g, and specific area is 150 ~ 400m
2/ g.
In the inventive method, adopt dipping solution I or dipping solution II when flooding, preferably adopt and saturatedly spray method, one or many can be adopted flood, all will through 200 DEG C or lower temperature drying after each dipping.In the inventive method, the concentration of maceration extract forms (content) by water absorption rate and required catalyst and determines.
Described alumina support can adopt conventional method to prepare, can containing a small amount of auxiliary agent as one or more in silicon, titanium, magnesium, boron, zirconium in alumina support, and auxiliary agent content counts 0.1% ~ 10% of carrying alumina body weight with element.The character General Requirements of described alumina support is as follows: pore volume is 0.3 ~ 1.5ml/g, and specific area is 150 ~ 450m
2/ g.
The inventive method adopts substep to spray method, first loads in catalyst carrier by least one in group vib metal, Organic Alcohol and organic sugar, and then group VIII metal and organic acid is loaded in catalyst carrier.The method can when organic compound consumption be less, the more weak Organic Alcohol (sugar) of complexing is first adopted to flood with the maceration extract of group vib metal, utilize the polarity of Organic Alcohol (sugar), group vib metal is made first to be dispersed in carrier surface, the stronger organic acid of complexing and part group VIII metal is adopted to form appropriate complex compound afterwards further, be conducive to group VIII metal be combined with the height of group vib metal and disperse on the alumina support, form the state of easier sulfuration, make VIB, group VIII metal obtains quick full cure, be conducive to VIB and form the active phase of more II class with group VIII metal, thus make catalyst have higher hydrogenation activity.In addition, in dipping solution, the consumption of organic compound is less, makes maceration extract not have higher viscosity, and this makes preparation become more easily to implement.
The inventive method, the VIII/(VIB+VIII that preferred employing is higher) weight ratio, and group vib and Organic Alcohol (sugar), group VIII and organic acid substep spray method on alumina support, when organic compound consumption is less, make catalyst have higher hydrogenation activity.
Catalyst for hydrogenation of fraction oil of the present invention is applicable to the cuts such as liquefied gas, gasoline, kerosene, diesel oil, wax oil, is particularly useful in diesel hydrogenation for removal sulphur technique.
Detailed description of the invention
In the present invention, specific area and pore volume adopt low temperature liquid nitrogen determination of adsorption method.In the present invention, wt% represents mass fraction.
Below in conjunction with embodiment, the present invention is further detailed explanation.
Embodiment 1
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, the aqueous solution of 0.9g ethylene glycol, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, at 110 DEG C dry 5 hours.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 15.3g basic cobaltous carbonate to rolling, 3.8g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst A.
Embodiment 2
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 21.5g molybdenum trioxide, the aqueous solution of 0.9g ethylene glycol, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, at 110 DEG C dry 5 hours.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 17.4g basic cobaltous carbonate to rolling, 3.5g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst B.
Embodiment 3
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, the aqueous solution of 2.0g glycerine, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, at 110 DEG C dry 5 hours.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 15.3g basic cobaltous carbonate to rolling, 2.4g grass aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst C.
Embodiment 4
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 2.5g molybdenum trioxide, 13.7g ammonium metatungstate, the aqueous solution of 0.8g ethylene glycol, after solution has sprayed, is rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 14.2g basic nickel carbonate to rolling, 3.7g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst D.
Embodiment 5
On 200ml fixed bed small hydrogenation device, adopt A, B, C, D catalyst respectively, the volume space velocity 2.0h when hydrogen dividing potential drop 4.0MPa, liquid
-1, hydrogen to oil volume ratio is 300Nm
3/ m
3, average reaction temperature is under 350 DEG C of conditions, the hydrotreatment of his-and-hers watches 1 Raw.
Table 1 feedstock property
| Feedstock oil | Atmosphere 3rd side cut straight-run diesel oil |
| Density (20 DEG C), g/cm 3 | 0.8533 |
| Boiling range (ASTM-D86), DEG C | |
| IBP/10% | 217/277 |
| 30%/50% | 296/309 |
| 70%/90% | 327/356 |
| 95%/FBP | 369/375 |
| Sulfur content, μ g/g | 17750 |
| Nitrogen content, μ g/g | 140 |
Comparative example 1
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, 18.7g basic cobaltous carbonate, 0.9g ethylene glycol, 4.7g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst E.
Comparative example 2
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, 18.7g basic cobaltous carbonate, 13.0g grass aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst F.
Comparative example 3
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, 18.7g basic cobaltous carbonate, the aqueous solution of 7.7g ethylene glycol, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst G.
Comparative example 4
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 21.9g molybdenum trioxide, 10.1g basic cobaltous carbonate, 0.8g ethylene glycol, 4.5g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst H.
Comparative example 5
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 22.9g molybdenum trioxide, 1.2g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, at 110 DEG C dry 5 hours.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 15.3g basic cobaltous carbonate to rolling, 3.8g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst I.
Comparative example 6
100g alumina support is placed in and rolls pot, under rotation condition, spray into 80ml to the alumina support rolled in pot with atomizing type and contain 21.9g molybdenum trioxide, the aqueous solution of 0.8g ethylene glycol, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, at 110 DEG C dry 5 hours.Be placed in again after taking weight and roll pot, under rotation condition, spray into 35ml with atomizing type again in pot contain 8.3g basic cobaltous carbonate to rolling, 3.7g lemon aqueous acid, after solution has sprayed, be rotated further 30 minutes rolling in pot, then place 18 hours, drying 5 hours at 110 DEG C, obtained finished catalyst J.
Comparative example 7
Evaluate catalysts E, F, G, H, I, J respectively, evaluation method is with embodiment 4.
Embodiment 6
The comparing result that this example operates 600 hours for above each routine institute controlling catalyst physico-chemical property and above each example on small hydrogenation device is in table 2,3.
Table 2 catalyst main character
| Catalyst is numbered | A | B | C | D |
| Catalyst property | ||||
| MoO 3，wt% | 17.0 | 16.0 | 17.0 | 2.0 |
| CoO，wt% | 8.0 | 9.0 | 8.0 | - |
| NiO，wt% | - | - | - | 6.0 |
| WO 3，wt% | - | - | - | 11.0 |
| C，wt% | 1.5 | 1.4 | 1.2 | 1.5 |
| From organic acid C/ VIII metal molar ratio | 0.16 | 0.13 | 0.23 | 0.21 |
| From the C/ vib metal mol ratio of Organic Alcohol | 0.05 | 0.06 | 0.14 | 0.10 |
| CoO /(CoO+MoO 3) weight ratio | 0.32 | 0.36 | 0.32 | |
| NiO/(NiO+MoO 3+WO 3) weight ratio | - | - | - | 0.32 |
| Preparation method | The present invention | The present invention | The present invention | The present invention |
| Pore volume, ml/g | 0.36 | 0.37 | 0.37 | 0.35 |
| Specific area, m 2/g | 244 | 245 | 247 | 238 |
| Bulk density, g/ml | 0.90 | 0.90 | 0.89 | 0.86 |
| Intensity, N/ unit | 205 | 207 | 212 | 208 |
Continued 2
| Catalyst is numbered | E | F | G | H | I | J |
| Catalyst property | ||||||
| MoO 3，wt% | 17.0 | 17.0 | 17.0 | 17.0 | 17.0 | 17.0 |
| CoO，wt% | 8.0 | 8.0 | 8.0 | 4.5 | 8.0 | 4.5 |
| NiO，wt% | - | - | - | - | - | - |
| WO 3，wt% | - | - | - | - | - | - |
| C，wt% | 1.5 | 2.6 | 2.6 | 1.5 | 1.5 | 1.5 |
| From organic acid C/ VIII metal molar ratio | 0.16 | 1.02 | - | 0.21 | 0.16 | 0.21 |
| From the C/ vib metal mol ratio of Organic Alcohol | 0.05 | - | 0.46 | 0.05 | - | 0.05 |
| From organic acid C/ vib metal mol ratio | - | - | - | - | 0.05 | - |
| CoO /(CoO+MoO 3) weight ratio | 0.32 | 0.32 | 0.32 | 0.21 | 0.32 | 0.21 |
| NiO/(NiO+MoO 3+WO 3) weight ratio | ||||||
| Preparation method | Total immersion method | Total immersion method | Total immersion method | Total immersion method | Sub-dip method | Sub-dip method 5--> |
| Pore volume, ml/g | 0.34 | 0.35 | 0.35 | 0.38 | 0.35 | 0.39 |
| Specific area, m 2/g | 208 | 201 | 203 | 210 | 217 | 212 |
| Bulk density, g/ml | 0.90 | 0.91 | 0.91 | 0.87 | 0.89 | 0.88 |
| Intensity, N/ unit | 175 | 184 | 186 | 189 | 192 | 195 |
The activity level of table 3 catalyst
| Catalyst is numbered | A | B | C | D | E | F | G | H | I | J |
| Process conditions | ||||||||||
| Hydrogen dividing potential drop, MPa | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 | 4.0 |
| Volume space velocity, h -1 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 | 2.0 |
| Reaction temperature, DEG C | 350 | 350 | 350 | 350 | 350 | 350 | 350 | 350 | 350 | 350 |
| Generate oil nature | ||||||||||
| Sulphur, μ g/g | 288 | 286 | 292 | 307 | 328 | 390 | 386 | 366 | 322 | 329 |
| Nitrogen, μ g/g | 9.8 | 9.1 | 9.4 | 8.2 | 14.6 | 25.6 | 24.9 | 20.1 | 13.2 | 14.9 |
Table 3 result shows, catalyst of the present invention has better hydroprocessing activity, and comparatively comparative catalyst has better ultra-deep desulfurization, nitrogen removal performance.
Claims (9)
1. the preparation method of a catalyst for hydrogenation of fraction oil, described catalyst take aluminium oxide as carrier, with at least one group vib metal and at least one group VIII metal for hydrogenation active metals, group VIII metal/(group vib metal+group VIII metal) with the weight ratio of oxide basis for 0.30 ~ 0.55, containing organic compound in catalyst, organic compound comes from organic acid and is selected from least one in Organic Alcohol and organic sugar, this catalyst adopts infusion process load regulation group vib metal on the alumina support, group VIII metal and organic compound, the addition of organic compound accounts for the 1.0wt% ~ 1.8wt% of hydrotreating catalyst weight in C, process comprises:
(1) dipping solution I and dipping solution II is prepared respectively, wherein dipping solution I is formulated by containing group vib metal and at least one be selected from Organic Alcohol and organic sugar and water, dipping solution II is by formulated containing group VIII metallic compound and organic acid, water, wherein organic acid addition is in the mol ratio of C and group VIII metal for 0.01 ~ 0.70, is selected from least one in Organic Alcohol and organic sugar in the mol ratio of C and group vib metal for 0.01 ~ 0.40;
(2) first use dipping solution I oxide impregnation alumina supporter, at the temperature of less than 200 DEG C after drying, then flood with dipping solution II, dry at the temperature of less than 200 DEG C, obtain hydrotreating catalyst.
2. in accordance with the method for claim 1, it is characterized in that in described hydrotreating catalyst, with the weight of catalyst for benchmark, hydrogenation active metals with the weight content of oxide basis for 14% ~ 50%.
3. in accordance with the method for claim 1, it is characterized in that in described hydrotreating catalyst, with the weight of catalyst for benchmark, hydrogenation active metals with the weight content of oxide basis for 15% ~ 40%.
4. in accordance with the method for claim 1, it is characterized in that, in described hydrotreating catalyst, group vib metal is Mo and/or W, group VIII metal is Ni and/or Co.
5. in accordance with the method for claim 1, it is characterized in that the addition of described organic compound accounts for the 1.2wt% ~ 1.6wt% of hydrotreating catalyst weight in C.
6. in accordance with the method for claim 1, it is characterized in that described organic acid is selected from carbon number is at least one in the binary acid of 2 ~ 10; Described Organic Alcohol be selected from carbon number be 3 ~ 10 fatty alcohol and dihydroxylic alcohols in one or more; It is the monose of 3 ~ 10, at least one in disaccharides and polysaccharide that described organic sugar is selected from carbon number.
7. in accordance with the method for claim 1, it is characterized in that described organic acid is one or more in citric acid, citric anhydride, isocitric acid, malic acid, tartaric acid, oxalic acid, butanedioic acid, glutaric acid, adipic acid, benzoic acid, phthalandione, isophathalic acid, salicylic acid, malonic acid; Described Organic Alcohol is one or more in ethylene glycol, propyleneglycoles, glycerine, three methylol ethane, three methylol propane, divinyl ethylene glycol, two propyleneglycoles, trimethylene ethylene glycol, trietbhlene glycol, tributylene glycol, four ethylene glycols, tetrapropylene ethylene glycol, polyethylene glycol, divinyl Propylene Glycol, divinyl ethohexadiol, divinyl propyl glycol, divinyl butyl glycol; It is the monose of 3 ~ 10, at least one in disaccharides and polysaccharide that described organic sugar is selected from carbon number.
8. in accordance with the method for claim 1, it is characterized in that weight content is in the catalyst 0.01% ~ 2.5% containing phosphorus in described hydrotreating catalyst.
9. in accordance with the method for claim 1, it is characterized in that: adopt dipping solution I or dipping solution II when flooding, adopt and saturatedly spray method, adopt one or many dipping, all will through the temperature drying of less than 200 DEG C after each dipping.
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| CN108620082B (en) * | 2017-03-24 | 2019-09-10 | 中国石油化工股份有限公司 | The preparation method of hydrogenation catalyst |
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| CN100448538C (en) * | 2004-10-29 | 2009-01-07 | 中国石油化工股份有限公司 | Distillate hydrogenation catalyst and its preparation method |
| CN1966615B (en) * | 2005-11-16 | 2012-07-04 | 中国石油化工股份有限公司 | Hydrogenation catalyst |
| CN101210198B (en) * | 2006-12-27 | 2012-03-21 | 中国石油化工股份有限公司 | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material |
| CN101722039B (en) * | 2008-10-21 | 2011-08-10 | 中国石油化工股份有限公司 | Hydrogenation catalyst and preparation method thereof |
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