CN1448477A - Heavy raw oil hydrogenating treatment catalyst and its preparing method - Google Patents
Heavy raw oil hydrogenating treatment catalyst and its preparing method Download PDFInfo
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Abstract
The present invention discloses one kind of catalyst for the hydrotreatment of heavy material oil and its preparation. The catalyst consists of fluorine 0.5-15 wt%, assistant M in oxide 1.0-30 wt%, VIB metal oxide 15-35 wt%, VIII metal oxide 2.0-10 wt% and alumina the rest. It features the simultaneous modification of catalyst carrier with both fluorine and assistant M, and this can not only regulate the physical and chemical property of catalyst but also avoid the loss of fluorine in the catalyst, which will lower the activity of the catalyst, corrode the downstream apparatus and pollute environment. The catalyst is used in hydrotreatment of heavy material oil and has excellent hydrodesulfurizing, hydrodenitrifying and arene saturating performance.
Description
1, technical field
The present invention relates to a kind of hydrotreating catalyst and preparation method thereof, particularly contain heavy raw oil hydrogenating treatment catalyst of fluorine auxiliary agent and preparation method thereof.
2, background technology
In recent years; crude oil heaviness, poor qualityization tendency become clear day by day in the world wide; requirement on environmental protection increasingly stringent on the other hand; quality to processed oil has proposed more and more stricter standard; particularly require in the oil product content of sulphur and aromatic hydrocarbons more and more lower, force the dealer to continually develop and use various performances better to be suitable for the high-activity hydrogenation catalyst of heavy raw oil.
Aromatic hydrocarbons in the heavy raw oil mainly is polycyclic aromatic hydrocarbons, the aromatic hydrogenation saturated reaction mainly is that polycyclic aromatic hydrocarbons hydrogenation and open loop form the less mononuclear aromatics of number of rings or the reaction of double ring arene, owing to relate to the ring-opening reaction of aromatic hydrocarbons, require acidity of catalyst stronger, have certain lytic activity; And the sulphur in the heavy raw oil, nitrogen mainly is that the form with the polynuclear aromatics derivative exists, such as: the dibenzothiophene of replacement, contain substituent carbazole, dibenzopyridine etc., because polynuclear aromatics stability and have the reaction compartment steric hindrance, make sulphur, nitrogen-atoms generation hydrogenolysis, it is sterically hindered to reduce at first must to make polycyclic aromatic hydrocarbons that certain ring-opening reaction takes place, help the generation of hydrogenolysis, therefore, no matter for heavy raw oil is hydrogenating desulfurization, hydrodenitrification still is that the aromatic hydrogenation saturated reaction all requires the activity of such catalysts component to have good hydrogenation performance, require catalyzer to have certain cracking performance simultaneously, require catalyzer to have certain acidity like this, because the green coke reaction easily takes place and coking deactivation in L acid (Lewise acid), thereby mainly is that the requirement catalyzer has certain B acid (Br ō nsted acid).And the acidity of catalyzer depends primarily on the acidity of support of the catalyst, aluminum oxide is big because of its cheapness, easy-formation, specific surface area, physico-chemical property such as pore volume, aperture can be adjusted within very wide scope, thereby be widely used for preparing the carrier of hydrogenation catalyst, but a little less than the simple alumina supporter acidity, and mainly be L acid, B acid is very weak, exist easily and hydrogenation activity component generation strong interaction and the shortcoming of non-activity species of forming, for example aluminum oxide easily with nickel formation nickel aluminate, the active ingredient sintering easily takes place and influence activity of such catalysts, stability etc.
Above-mentioned shortcoming and defect at aluminum oxide, usually add the acidity that auxiliary agent improves support of the catalyst, inhibited oxidation aluminium and hydrogenation activity component generation strong interaction, slow down the sintering velocity of active ingredient, improve dispersiveness, reductibility and the curability of active ingredient, finally reach the purpose that improves catalyst activity at carrier surface; The adding of auxiliary agent is played toward contact and is prolonged catalyzer work-ing life, raising selectivity and stable effect.
In patent CN1002090 and CN1056514, all adopt at alumina surface dipping fluorine auxiliary agent and improve the surface properties of aluminum oxide, the purpose that the raising acidity of catalyst finally reaches raising catalyst hydrogenation activity and lytic activity.Adopting fluorine-containing solution to carry out isomorphous substitution among patent US5139648 and the US5080778 reacts and prepares fluorizated silica-alumina supports or fluorizated alumina supporter, the metal component of load with hydrogenation activity makes catalyzer then, and this catalyzer is mainly used in the cracking conversion process of heavy carbon hydrocarbon molecule.Be carrier with silicon oxide and aluminum oxide mixed oxide among the patent US4427534, flood the hydrogenation activity that the fluorine auxiliary agent promotes tungsten and nickel active ingredient then, this catalyzer has the saturated performance of higher hydrogenating desulfurization, hydrodenitrification and aromatic hydrocarbons, is mainly used in the production of rocket engine fuel and diesel oil.All adopt fluorine to improve the character of carrier and catalyzer as auxiliary agent in the above patent, but they all do not relate to the fluorine losing issue in the catalyzer, after fluorine in the catalyzer runs off, can produce following unfavorable result: 1. the reduction of fluorine content causes that activity of such catalysts descends, 2. the fluorine corrosion upstream device that runs off, 3. the fluorine of Liu Shiing is taken out of with product and contaminate environment.
3, summary of the invention
The objective of the invention is to shortcoming and defect, propose a kind of heavy raw oil hydrogenating treatment catalyst and preparation method thereof, make that the fluorine in the catalyzer is difficult for running off at above-mentioned prior art.
The invention discloses a kind of heavy raw oil hydrogenating treatment catalyst and preparation method thereof, contain fluorine and auxiliary agent M (auxiliary agent M is one or more among Si (silicon), Ti (titanium), Zr (zirconium), the B (boron)), VIB (Mo, W) family and VIII (Fe, Co, Ni) family's active ingredient in this catalyzer.Wherein fluorine and auxiliary agent M add to mix the mode of pinching in the process of support of the catalyst moulding, take mode load regulation VIB (Mo, W) family and VIII (Fe, Co, Ni) family's active ingredient of flooding on shaping carrier.Its effect is that fluorine is difficult for running off in this catalyzer.This catalyzer can be used as the hydrotreatment process of heavy raw oil, has good hydrogenating desulfurization, hydrodenitrification, the saturated performance of aromatic hydrocarbons.
By the fluorine-containing heavy raw oil hydrogenating treatment catalyst of the inventive method preparation, character is as follows:
Quality with catalyzer is a benchmark, consist of: fluorine 0.5～15m%, auxiliary agent M be in oxide form 1.0～30m%, VIB (Mo, W) family metal oxide 1 5～35m%, VIII (Fe, Co, Ni) family metal oxide 2.0～10m%, all the other are aluminum oxide; Wherein auxiliary agent M is one or more among Si (silicon), Ti (titanium), Zr (zirconium), the B (boron), and auxiliary agent M is preferably Si (silicon), with SiO
2Form is calculated content and is preferably 2.0～15m%; The preferable range of all the other each component concentrations is in this catalyzer: fluorine 1.0～6.0m%, group vib metal oxide 15～30m%, group VIII metal oxide 3.0～8.0m%.The difficult fluorine retentivity that runs off or be called in the catalyzer of fluorine is good in the catalyzer of the present invention, and concrete description is to heat 200 hours under 450 ℃ of temperature in air atmosphere, and the fluorine turnover rate in the catalyzer is lower than 5.0%, generally speaking between 0.5～5.0%.
Pore structure character: pore volume 0.20～0.70ml/g, specific surface area 100～300m
2/ g.
The acid amount of catalyzer, characterizes with infrared spectra as probe molecule with pyridine, and the acid amount is: B acid 0.10～0.35mmol/g, L acid 0.10～0.30mmol/g.
The preparation method of fluorine-containing heavy raw oil hydrogenating treatment catalyst of the present invention:
Get aluminum oxide or aluminum hydroxide solid elastomer powder, add additive, water, peptizing agent, fluorochemicals and contain the even aftershaping of compound of second kind of auxiliary agent M, then drying, roasting and make desired fluorine-containing support of the catalyst; Again with the solution that contains VIB (Mo, W) family, VIII (Fe, Co, Ni) family metallic element compound flood, drying and calcination activation make fluorine-containing heavy raw oil hydrogenating treatment catalyst of the present invention.
Describe the preparation method of the fluorine-containing heavy oils oil hydrogenating treatment catalyst of the present invention below in detail:
(1) get required aluminum hydroxide solid elastomer powder or aluminum oxide dry glue powder, additive, the compound that contains auxiliary agent M, fluorochemicals and water, these raw materials kneadings evenly are the paste plastic, moulding on shaper then, drying, roasting make support of the catalyst.
(2) prepare the solution that contains VIB (Mo, W) family, VIII (Fe, Co, Ni) family metallic element compound, with this solution impregnation said catalyst carrier, drying, calcination activation can make catalyzer of the present invention.
In the step of above-mentioned preparation catalyzer, with the aluminum oxide butt is benchmark, the consumption of each material, additive accounts for 2.0～15m%, fluorochemicals accounts for 1.0～30m%, the compound (in pure compound) that contains auxiliary agent M accounts for 1.0～40m%, and water accounts for 50～70m% in above whole mixture, deducts moisture content contained in each material and both has been the water yield of required adding; The consumption that contains VIB (Mo, W) family, VIII (Fe, Co, Ni) family metallic element compound according to the amount of support of the catalyst adsorbent solution and the catalyst activity components contents that requires, calculates according to a conventional method.
Also can add peptizing agent in the kneading process of step (1), add-on is 2.0～10m%.When the aqueous solution of fluorochemicals is acidity, can reduces and even not use peptizing agent.
The aluminum hydroxide solid elastomer powder that adopts in the Preparation of catalysts method mainly is meant boehmite and pseudo-boehmite, and aluminum oxide is meant γ-Al
2O
3, η-Al
2O
3, θ-Al
2O
3Dry glue powder.
The additive that adopts in the Preparation of catalysts method (or being called the moulding additive) is meant the material that helps moulding, such as sesbania powder, carbon black, Graphite Powder 99, macromolecular organic compound (such as methylcellulose gum, cellulose acetate etc.), gelatin etc.The main purpose of adding these materials is to help shaping of catalyst, improves the intensity of catalyzer, improves the efficient of moulding, also may produce some other little effect simultaneously, the influence that the pore structure of catalyzer is produced microcosmic.
The fluorochemicals that adopts in the Preparation of catalysts method mainly is meant ammonium silicofluoride, Neutral ammonium fluoride, hydrofluoric acid, boron fluoride etc., wherein be preferred with the ammonium silicofluoride, this raw material has following advantage: the source that 1. fluorine and silicon are provided simultaneously, 2. ammonium silicofluoride is soluble in water, help obtain solution and make and be uniformly dispersed, 3. the aqueous solution is acidity and can partly or entirely replaces peptizing agent.
The preparation peptizing agent that catalyzer adopted can be a mineral acid, as: nitric acid, phosphoric acid, hydrofluoric acid etc., organic acid, as: formic acid, acetate, oxalic acid, citric acid etc., strongly-acid anion salt soluble in water, such as: aluminum nitrate, Tai-Ace S 150, ammonium silicofluoride etc.
The compound that contains second kind of auxiliary agent M mainly is meant the compound of one or more elements among Si (silicon), Ti (titanium), Zr (zirconium), the B (boron), serve as preferred wherein to contain Si (silicon) compound, silicon-containing compound can be the mineral compound of silicon, as: silicon-dioxide, silicon sol, silicon gel etc.; The organic compound of silicon is such as tetraethyl silicate, methyl silicate etc., and preferably adopting the silicon sol of low sodium element is raw material.
The introducing mode that contains second kind of auxiliary agent M compound in the catalyst preparation step can be: 1. when containing auxiliary agent M compound and be solid state powder, aluminium hydroxide or aluminum oxide dry glue powder, contain auxiliary agent M compound and additive is mixed together evenly, and then add the solution that fluorochemicals and peptizing agent are arranged; 2. when containing auxiliary agent M compound and be water-soluble material, get portion water, add then in the mixture that has mixed this compound dissolution; 3. or containing auxiliary agent M compound be mixed with mixing solutions with fluorochemicals, add in the mixture then.
The forming method of catalyzer of the present invention mainly refers to industrial forming method commonly used, as extruded moulding, beat methods such as sheet (compressing tablet) moulding, spin.Catalyst appearance can be different because of forming method with size, adopt different experiment conditions to change, as adopt the orifice plate of the replaceable banded extruder of extruded moulding and realize easily, can obtain cylinder shape, trifolium-shaped, Herba Galii Bungei type, special special-shaped bar etc., play the sheet moulding and can realize that size of catalyst can be between 0.5mm～20mm because of the shape that changes mould.
The preparation catalyzer related solution that contains VIB (Mo, W) family, VIII (Fe, Co, Ni) family metallic element compound is to be mixed to stir with water or ammoniacal liquor and made by contain VIB (Mo, the W) family, VIII (Fe, Co, Ni) family metallic element compound of water-soluble or ammonia dissolubility.Wherein VIB (Mo, W) the family the most effective source of metallic element compound is ammonium molybdate, molybdic oxide, ammonium metawolframate, metatungstic acid nickel etc., and VIII (Fe, Co, Ni) family metallic element compound can be selected from iron nitrate, iron acetate, Xiao Suangu, Cobaltous diacetate, cobaltous dihydroxycarbonate, basic nickel carbonate, nickelous nitrate, nickel acetate, single nickel salt, nickelous chloride etc.Be mainly used in the hydrodesulfurization reaction of stock oil when catalyzer, can select Co-Mo type active ingredient for use, tend to the aromatic hydrogenation saturated reaction of raw material, can adopt Ni-W type active ingredient, if the temperature of reaction of hydrogenation is higher, preferably adopt Ni-Mo type active ingredient or Ni-Mo-W type active ingredient, more help the hydrofining effect of raw material.
Pickling process can adopt saturated pickling process (be also referred to as and do dipping), also can adopt the supersaturation pickling process.Saturated pickling process is to form good required active component solution amount and the concentration of calculating according to the water-intake rate of carrier and catalyzer, adopt the mode of spray in rotary container, to carry out then, treat to rotate 20～40 minutes after solution spraying finishes, drying, roasting make catalyzer then again; The supersaturation pickling process uses the active component solution of 2～4 times of volumes of carrier adsorbent solution amount to soak support of the catalyst 0.5～6 hour, carries out solid-liquid separation, drying, roasting then and gets final product.
The drying of preparation catalyzer is between 80～130 ℃ dry 1～10 hour, and wherein the exsiccant time is because of the different variations to some extent with the catalyzer bed thickness of exsiccant temperature.
The roasting of preparation catalyzer can be between 500～900 ℃ roasting 1～20 hour, also can be the segmentation roasting, at first roasting 1～10 hour between 200～400 ℃, roasting between 500～900 ℃ then.
Outside the defluorination auxiliary agent, following advantage is found in the introducing of second kind of auxiliary agent M at least in the catalyzer: 1. adjust the ratio of F/M, and the content of auxiliary agent M.2. introduce the loss that second kind of auxiliary agent M can prevent fluorine afterwards effectively.Thereby the loss that has solved fluorine causes problems such as catalyst activity reduction, corrosion upstream device, contaminate environment.3. introduce the pore structure character that second kind of auxiliary agent M can improve catalyzer afterwards.For example use the raw material of ammonium silicofluoride as the fluorine auxiliary agent, though can provide fluorine and silicon simultaneously, if merely only add ammonium silicofluoride, the ratio of adjusting F/Si is very difficult, by improving the amount that maturing temperature or change time can finely tune F, but effect is undesirable, when too high maturing temperature can make the part fluorine burn the carrier hole structure is produced adverse influence, if add after the silicon compound, the ratio of F/Si is easy to adjust; Merely adopt ammonium silicofluoride on the other hand, particularly during the large usage quantity of ammonium silicofluoride, the pore structure of alumina supporter is destroyed obviously, show that mainly pore volume reduces, specific surface area reduces, and introduce the introducing of the compound, particularly silicon sol contain second kind of auxiliary agent M, and silicon sol prior to or simultaneously and ammonium silicofluoride join the effect that can play reaming in aluminum oxide or the aluminium hydroxide effectively together.
Have good effect by fluorine-containing heavy feed stock oil hydrogenation catalysts of the present invention:
1) fluorine in the catalyzer is difficult for running off.
2) physico-chemical property of catalyzer can be adjusted within limits.
Can in 0.10～0.35mmol pyridine/g scope, regulate as catalyst B acid amount.Fluorine and auxiliary agent M form and the ratio scope of F/M is F/M=20～0.10: 1 in the catalyzer, and when second kind of auxiliary agent M was Si, the ratio of the amount of substance of fluorine silicon can be at F/Si=10～adjust between 0.20: 1.
3) as the hydrotreating catalyst of heavy raw oil, the hydrogenating desulfurization of catalyzer, hydrodenitrification
The saturated performance of aromatic hydrocarbons is good.
After fluorine-containing heavy raw oil hydrogenating treatment catalyst of the present invention adopts vulcanizing agent to carry out prevulcanized catalyzer is changed into sulphided state by oxidation state, promptly can be used for the hydrotreatment of heavy distillate, the hydrotreatment of lubricating oil, the hydroconversion process of residual oil, the hydrofining treating processes that also can be used for general distillate, the hydrogenation pre-refining process of white oil, Vaseline, petroleum wax, Microcrystalline Wax (ceresine).Be used for the processing treatment process of above all kinds of oil products by the catalyzer of method disclosed by the invention preparation, hydrogenating desulfurization, hydrodenitrification, aromatic hydrocarbons saturation effect are good, and product that can the production environment close friend has good economic and social benefit.
4, embodiment
Embodiment 1
Method with extruded moulding is the preparation process that example is introduced support of the catalyst.
Get silicon sol 8.5ml (SiO
230m%), ammonium silicofluoride 10g and water 80ml are mixed with solution; Aluminium hydroxide dry powder 100g, carbon black 10g and sesbania powder 5.0g are mixed, add above-mentioned solution and be kneaded into uniform plastic, extruded moulding is the cloverleaf pattern bar of 1.2mm, 120 ℃ of dryings 4 hours, 600 ℃ of roasting temperatures 4 hours, can obtain fluorine-containing support of the catalyst A.
Get silicon sol 30ml, acetum 2.0ml (HAc 36%), ammonium silicofluoride 8.0g and water 75ml and be mixed with solution; Aluminium hydroxide dry powder 100g, carbon black 10g and sesbania powder 5.0g are mixed, add above-mentioned solution and be kneaded into uniform plastic, extruded moulding is the cylinder shape bar of 1.5mm, 110 ℃ of dryings 4 hours, 650 ℃ of roasting temperatures 4 hours, can obtain fluorine-containing support of the catalyst B.
Get ammonium silicofluoride 8.0g, acetum 1.0ml and water 85ml and be mixed with fluorine-containing solution; Aluminium hydroxide dry powder 100g, carbon black 10g and sesbania powder 5.0g are mixed, adding silicon sol 7.0ml mixes, adds above-mentioned fluorine-containing solution and is kneaded into uniform plastic earlier, extruded moulding is the Herba Galii Bungei shape bar of 1.2mm, 120 ℃ of dryings 4 hours, 600 ℃ of roasting temperatures 4 hours, can obtain fluorine-containing support of the catalyst C.
Get ammonium silicofluoride 5.0g, acetum 2.0ml and water 80ml and be mixed with fluorine-containing solution; Aluminium hydroxide dry powder 100g, boric acid 4.5g, carbon black 10g and sesbania powder 5.0g are mixed, add fluorine-containing solution again and be kneaded into uniform paste plastic, extrusion molding is the cylinder shape bar of 1.5mm, 110 ℃ of dryings 3 hours, 400 ℃ of roasting temperatures 3 hours, 700 ℃ of roasting temperatures 4 hours, can obtain fluorine-containing support of the catalyst D.
Embodiment 2
Present embodiment has been introduced the preparation and the Preparation of Catalyst of active component solution.
Get 203g nickelous nitrate (Ni (NO
3)
26H
2O), the 320g ammonium metawolframate (contains WO
385.2m%), be mixed with 500ml tungsten nickel solution after adding deionized water and stirring dissolving.
The carrier A of getting among this tungsten nickel solution 40ml and the 50g embodiment 1 places rotary drum to spray (saturated pickling process), and the time of spraying is 30 minutes, has sprayed the back taking-up and has dried 3 hours down at 120 ℃, then 500 ℃ of following roastings 3 hours, makes catalyst A 1.
Get the support C among the embodiment 1, flooded (supersaturation pickling process) 2 hours, filter, dried 3 hours down,, make catalyzer C1 then 450 ℃ of following roastings 3 hours at 110 ℃ with above-mentioned tungsten nickel solution 200ml.
Get 56g basic nickel carbonate (containing NiO 44.7m%), the 152g ammonium molybdate (contains MoO
382.7m%), add ammoniacal liquor (concentration 11.2mol/l), be mixed with 500ml molybdenum nickel ammonia solution after heating, the stirring and dissolving.
The carrier B of getting among this molybdenum nickel ammonia solution 43ml and the 50g embodiment 1 places rotary drum to spray, and the time of spraying is 30 minutes, has sprayed the back taking-up and has dried 3 hours down at 120 ℃, then 500 ℃ of following roastings 3 hours, makes catalyst B 1.
The carrier D that gets among above-mentioned molybdenum nickel ammonia solution 150ml and the 50g embodiment 1 flooded 1 hour, filtered, and dried 5 hours down at 100 ℃, then 550 ℃ of following roastings 3 hours, made catalyzer D1.
Catalyst A l, B1, C1, D1 character are listed in the table 1.
Table 1: the character of catalyzer
*Annotate: the acid amount of catalyzer be with pyridine as probe molecule, infrared measurement in the time of 250 ℃, unit are mmol pyridine/g.
Comparing embodiment
Aluminium hydroxide dry powder 100g, acetic acid 5.2ml, carbon black 10g, sesbania powder 5.0g and water 75ml are kneaded into uniform plastic, and extruded moulding is the cloverleaf pattern bar of 1.2mm, and 120 ℃ of dryings 3 hours 600 ℃ of roasting temperatures 4 hours, make alumina supporter; Neutral ammonium fluoride 30g adds deionized water and is mixed with the 200ml aqueous solution, this solution impregnation of carrying alumina body and function (supersaturation pickling process) 4 hours, filter, 120 ℃ of dryings 4 hours were 600 ℃ of roasting temperatures 4 hours, make fluoro-containing alumina carrier E, place rotary drum to spray (saturated pickling process) with tungsten nickel solution 40ml among the embodiment 2 and 50g carrier E, the time of spraying is 30 minutes, has sprayed the back taking-up and has dried 3 hours down at 120 ℃, 500 ℃ of following roastings 3 hours, make catalyzer E1 then.
Getting the above-mentioned fluorine-containing catalyst A 1 that contains among fluorine catalyst E1 and the embodiment 2 heated 200 hours under 450 ℃ of temperature in air atmosphere, analyzed the variation before and after the fluorine content in the catalyzer is handled, experimental result is listed in the table 2, from the experimental result of table 2 as can be seen the fluorine turnover rate of catalyzer E1 far above the fluorine turnover rate of catalyst A 1, explanation is dipping fluorine auxiliary agent after the moulding of alumina supporter elder generation, flood the prior art scheme of active ingredient again, in the body formed process of carrying alumina, add simultaneously after fluorine and the second kind of auxiliary agents of silicon to mix the mode pinch with provided by the invention, the technical scheme of dipping active ingredient is compared: technical scheme provided by the invention has effectively prevented the loss of fluorine in the catalyzer.
Table 2: the result that fluorine runs off in the catalyzer
Application Example
Present embodiment has been introduced the hydrotreatment process that catalyzer C1 is applied to heavy raw oil.
Get catalyzer C1 among the embodiment 2 and according to a conventional method after the prevulcanized, carry out activity rating of catalyst with subtracting third fractional oil (VGO) for raw material (character is listed in table 3) with the kerosene that contains dithiocarbonic anhydride, test-results is listed in table 4.
Table 3: stock oil character
The stock oil title subtracts third fractional oil (VGO)
Density (20 ℃), kg/m
3956
Sulphur, m% 0.22
Nitrogen, m% 0.25
Mass spectrum is formed, m%
Stable hydrocarbon 59
Aromatic hydrocarbons 40
Boiling range, ℃
Initial boiling point 370
50％ 447
Final boiling point 508
Table 4: catalyzer C1 evaluation result
Reaction process condition
Volume space velocity h
-11.0 1.0
Hydrogen to oil volume ratio (v/v) 800 800
Pressure, MPa 8.0 12.0
Temperature, ℃ 300 360
Desulfurization degree, % 98.4 98.8
Denitrification percent, % 97.1 98.3
Take off fragrant rate, % 41.2 60.5
By the test evaluation result as can be seen, the fluorine-containing hydrotreating catalyst that is prepared by the inventive method has higher hydrogenating desulfurization, hydrodenitrification, the saturated performance of aromatic hydrocarbons, is specially adapted to the hydrofining treating processes of heavy raw oil.
Claims (13)
1. heavy raw oil hydrogenating treatment catalyst, it is characterized in that the quality with catalyzer is a benchmark, it consists of: fluorine 0.5～15m%, auxiliary agent M is in oxide form 1.0～30m%, group vib metal oxide 15～35m%, group VIII metal oxide 2.0～10m%, all the other are aluminum oxide; Wherein auxiliary agent M is one or more among Si, Ti, Zr, the B.
2. according to the described hydrotreating catalyst of claim 1, it is characterized in that said auxiliary agent M is Si, with SiO
2It is 2.0～15m% that form is calculated content.
3. according to the described hydrotreating catalyst of claim 1, it is characterized in that fluorine content is 1.0～6.0m% in this catalyzer, the group vib metal oxide is 15～30m%, and the group VIII metal oxide is 3.0～8.0m%.
4. according to the described hydrotreating catalyst of claim 1, it is characterized in that 450 ℃ were heated 200 hours down in air atmosphere, the fluorine turnover rate in the catalyzer is lower than 5.0%.
5. according to the described hydrotreating catalyst of claim 4, it is characterized in that 450 ℃ were heated 200 hours down in air atmosphere, the fluorine turnover rate in the catalyzer is between 0.5～5.0%.
6. according to the described hydrotreating catalyst of claim 1, it is characterized in that this catalyst pores textural property is: pore volume 0.20～0.70ml/g, specific surface area 100～300m
2/ g.
7. according to the described hydrotreating catalyst of claim 1, it is characterized in that the acid amount of catalyzer is: B acid 0.10～0.35mmol/g, L acid 0.10～0.30mmol/g.
8. the preparation method of a heavy raw oil hydrogenating treatment catalyst, it is characterized in that this method may further comprise the steps: (1) takes by weighing required aluminum hydroxide solid elastomer powder or aluminum oxide dry glue powder, additive, contains the chemical combination of auxiliary agent M
Thing, fluorochemicals and water are mediated evenly one-tenth paste plastic to these raw materials, then at shaper
Last moulding, drying, roasting make support of the catalyst; (2) prepare the solution that contains group vib, group VIII metallic element compound, urge with this solution impregnation is above-mentioned
Change agent carrier, drying, calcination activation can make catalyzer of the present invention;
The compound that wherein contains auxiliary agent M refers to the compound of one or more elements among Si, Ti, Zr, the B;
In the step of above-mentioned preparation catalyzer, with the aluminum oxide butt is benchmark, the consumption of each material, additive accounts for 2.0～15m%, fluorochemicals accounts for 1.0～30m%, the compound that contains auxiliary agent M accounts for 1.0～40m%, and water accounts for 50～70m% in above whole mixture, deducts moisture content contained in each material and both has been the water yield of required adding.
9. according to the described preparation method of claim 8, it is characterized in that also can adding peptizing agent in the raw material kneading process, add-on is that benchmark is 2.0～10m% with the aluminum oxide butt.
10. according to the described preparation method of claim 8, it is characterized in that said fluorochemicals refers to ammonium silicofluoride, Neutral ammonium fluoride, hydrofluoric acid, boron fluoride.
11., it is characterized in that the said compound that contains auxiliary agent M is a silicon-containing compound according to the described preparation method of claim 8.
12., it is characterized in that said silicon-containing compound is silicon-dioxide, silicon sol, silicon gel, tetraethyl silicate and/or methyl silicate according to the described preparation method of claim 11.
13. according to the described preparation method of claim 8, it is characterized in that the introducing mode that contains auxiliary agent M compound in catalyst preparation step is: 1. when containing auxiliary agent M compound and be solid state powder, aluminium hydroxide or aluminum oxide dry glue powder, contain auxiliary agent M compound and additive is mixed together evenly, and then add the solution that fluorochemicals is arranged; 2. when containing auxiliary agent M compound and be water-soluble material, get portion water, add then in the mixture that has mixed this compound dissolution; 3. or containing auxiliary agent M compound be mixed with mixing solutions with fluorochemicals, add in the mixture then.
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| CN100371077C (en) * | 2004-10-29 | 2008-02-27 | 中国石油化工股份有限公司 | Macropore alumina supporter and its preparation method |
| CN102600873A (en) * | 2012-03-05 | 2012-07-25 | 中国石油大学(华东) | Hydrotreatment catalyst and preparation method thereof |
| CN103506149A (en) * | 2013-09-18 | 2014-01-15 | 中国海洋石油总公司 | Preparation method of hydrocracking catalyst controlling active metal distribution |
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|---|---|---|---|---|
| CN102861601B (en) * | 2011-07-07 | 2015-08-26 | 中国石油化工股份有限公司 | A kind of fluorine-containing hydrogenation catalyst and preparation thereof |
| CN102861598B (en) * | 2011-07-07 | 2015-08-26 | 中国石油化工股份有限公司 | The hydrogenation catalyst of containing fluorin of active metal component non-uniform Distribution and preparation thereof |
-
2002
- 2002-04-04 CN CN 02109392 patent/CN1211464C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100371077C (en) * | 2004-10-29 | 2008-02-27 | 中国石油化工股份有限公司 | Macropore alumina supporter and its preparation method |
| CN102600873A (en) * | 2012-03-05 | 2012-07-25 | 中国石油大学(华东) | Hydrotreatment catalyst and preparation method thereof |
| CN103506149A (en) * | 2013-09-18 | 2014-01-15 | 中国海洋石油总公司 | Preparation method of hydrocracking catalyst controlling active metal distribution |
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| Publication number | Publication date |
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| CN1211464C (en) | 2005-07-20 |
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