CN104593067A - Method for producing white rubber filling oil base oil from catalytic slurry oil - Google Patents
Method for producing white rubber filling oil base oil from catalytic slurry oil Download PDFInfo
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- CN104593067A CN104593067A CN201310532430.3A CN201310532430A CN104593067A CN 104593067 A CN104593067 A CN 104593067A CN 201310532430 A CN201310532430 A CN 201310532430A CN 104593067 A CN104593067 A CN 104593067A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
Abstract
The invention discloses a method for producing white rubber filling oil base oil through catalytic slurry oil hydrogenation. The method comprises the following steps: catalytic slurry oil is subjected to fractionation, such that a light fraction and a heavy fraction are obtained; the light fraction is mixed with hydrogen, and the mixture enters a hydrogenation treatment reaction zone; the mixture sequentially contacts a hydrogenation protection catalyst, a hydro-refining catalyst and a hydro-upgrading catalyst A, such that a hydrogenation reaction is carried out; a hydrogenation treatment effluent enters a hydro-upgrading reaction zone; a hydro-upgrading catalyst B containing amorphous silica-alumina and modified Y zeolite is adopted in the hydro-upgrading reaction zone, and a hydro-upgrading reaction is carried out under the existence of hydrogen; a hydro-upgrading effluent enters a hydro-finishing reaction zone, and is subjected to a hydro-finishing reaction; and a hydro-finishing product is separated, such that the rubber filling oil base oil is obtained. According to the invention, the catalytic slurry oil is adopted as a raw material, and can be used for producing the white rubber filling oil base oil with good low-temperature fluidity, good intersolubility with rubber, and good oxidation stability.
Description
Technical field
The present invention relates to a kind of production method of rubber filling oil base oil, specifically a kind of catalytic slurry adopts the method for hydrotreatment-hydro-upgrading-hydrofinishing combined hydrogenation processing method production white rubber extending oil base oil.
Background technology
Naphthenic base crude produces rubber filling oil: for improving some performance of rubber, needing mineral oil to be filled with in synthetic rubber, thus it being called rubber filling oil.In synthetic rubber, usually containing benzene ring structure in rubber chain-like structure, according to similar principle of dissolving each other, hydrocarbon oil should be desirable rubber oil, is secondly exactly naphthenic oil.But due to the material that aromatic hydrocarbon oil is a kind of strong toxicity, along with people are grown to even greater heights to the cry of health, safety, environmental protection, and some expensive goods are as more and more higher in the requirement of sports shoes to rubber filling oil base oil, the use restriction for aromatic hydrocarbon oil can get more and more.Current western developed country, has formulated various restriction, has prohibitted the use the oil product containing aromatic hydrocarbon.So naphthenic oil becomes the preferably selection of rubber oil.
The production technique of rubber filling oil base oil is along with the development of oil refining process.Be using naphthenic base crude as raw material the earliest, adopt sulfuric acid sulfonation-clay-filtered explained hereafter rubber filling oil base oil, but the method cost be high, yield is low, treatment capacity is little, the most important thing is to produce a large amount of acid sludge contaminate environment.
CN201010222066.7 discloses a kind of method adopting perhydro method to produce rubber filling oil base oil.With cycloalkyl distillate for raw material, the one-stage serial hydrogenation technique of hydrotreatment-hydrodewaxing-hydrofinishing is adopted to produce rubber filling oil base oil and other specialty oil products.The method energy consumption is low, good product quality, but there is the problem of cycloalkyl distillate resource-constrained.
At present, the naphthenic base crude resource of China mainly concentrates on the large block in Karamay, Xinjiang, Liaohe Huanxiling and Bohai Sea Gulf three, wherein, at home and abroad share of market is higher to utilize the naphthenic rubber extending oil base oil of Karamay, Xinjiang crude production, and effect is better.And Liaohe Huanxiling crude oil reduces and quality variation along with output, can not as the stable resources producing rubber filling oil.Along with the development of China's rubber industry, the domestic rubber filling oil market requirement constantly increases, and imbalance between supply and demand is more outstanding, therefore opens up the rubber filling oil raw materials for production that other is suitable, realizes rubber filling oil and significantly domesticize, be of great immediate significance.
Petroleum refining industry of China has very large catalytic cracking processing power, 70% of gasoline, 30% blend component of diesel oil from catalytic cracking unit, the catalytic slurry that simultaneously by-product is a large amount of.Catalytic slurry due to sulphur, nitrogen content high, metal content is high, and aromatic hydrocarbons accounts for more than 50%, limits its application, except on a small quantity as other secondary processing process ginseng refining raw material, mostly burns as oil fuel, not only wastes resource, cause environmental pollution simultaneously.It is high that catalytic slurry has aromaticity content, after hydrotreatment and hydro-upgrading, can be transformed into naphthenic hydrocarbon, can produce the rubber filling oil base oil that low-temperature fluidity is good, solubility property is outstanding, oxidation stability is good.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of is raw material with catalytic slurry, adopts the method for the method production white rubber extending oil base oil of hydrotreatment-hydro-upgrading-hydrofinishing hydrogenation combination technique.
Catalytic slurry hydrogenation production white rubber extending oil base oil method of the present invention comprises following content:
(1) catalytic slurry obtains lighting end and last running through fractionation, and cut point is 480 ~ 510 DEG C;
(2) step (1) described lighting end enters hydrotreatment reaction zone after mixing with hydrogen, contacts successively carry out hydrogenation reaction with hydrogenation protecting catalyst, Hydrobon catalyst with catalyst for hydro-upgrading A;
(3) step (2) gained hydrotreatment effluent enters hydro-upgrading reaction zone, and hydro-upgrading reaction zone uses the catalyst for hydro-upgrading B containing amorphous aluminum silicide and modified Y zeolite, in presence of hydrogen, carries out hydro-upgrading reaction;
(4) step (3) gained hydro-upgrading effluent enters hydrofinishing reaction zone, in presence of hydrogen, with hydrofinishing catalyst exposure, carry out hydrofinishing reaction, hydrofinishing product is isolated to gasoline blending component, diesel oil blending component, white rubber extending oil base oil.
In the inventive method, step (1) described catalytic slurry carries out fractionation after first carrying out dewatering and remove mechanical impurity again.
In the inventive method, after the described catalytic slurry fractionation of step (1), gained last running can be used as modifying asphalt, heavy fuel oil (HFO), or is used as coking raw material.
In the inventive method; hydrotreatment reaction zone loads hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A from top to bottom; the admission space ratio of hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A is 10 ~ 60:20 ~ 70:20 ~ 70, is preferably 10 ~ 30:45 ~ 60:30 ~ 45.
In the inventive method; hydrotreatment reaction zone uses conventional hydrogenation protecting catalyst; the FZC series protective material of Fushun Petrochemical Research Institute (FRIPP) development and production can be adopted; also can conventionally prepare; these catalyzer generally with porous refractory inorganic oxide if aluminum oxide is for carrier; group vib and/or group VIII metal such as the oxide compound of W, Mo, Co, Ni etc. are active ingredient, optionally add other various auxiliary agent as the catalyzer of the elements such as P, Si, F, B.
In the inventive method, the Hydrobon catalyst that hydrotreatment reaction zone uses, can select this field general goods catalyzer, also can prepare by this area general knowledge.The commercial catalysts that can select as Fushun Petrochemical Research Institute (FRIPP) development and production 3936,3996, the Hydrobon catalyst such as FF-16, FF-26.
In the inventive method, hydrotreatment reaction zone uses the catalyst for hydro-upgrading A containing amorphous aluminum silicide and modified Y zeolite.Contain in described catalyst for hydro-upgrading A: the group VIII metal (with oxide basis) of the modified Y zeolite of 10wt% ~ 35wt% amorphous aluminum silicide, 2wt% ~ 15wt%, the group VIB metal (with oxide basis) of 20wt% ~ 50wt% and 8wt% ~ 15wt%.The character of amorphous aluminum silicide wherein used is as follows: silicon oxide-containing 20wt% ~ 70wt%, and specific surface is 350 ~ 600m
2/ g, pore volume is 1.0 ~ 2.0mL/g, and infrared acidity is 0.20 ~ 0.40mmol/g, and the pore volume that the pore volume of bore dia 4 ~ 10nm accounts for 85% ~ 95%, >15nm of total pore volume accounts for less than 5% of total pore volume; Preferred property is as follows: silicon oxide-containing 25wt% ~ 40wt%, and specific surface is 500 ~ 630m
2/ g, pore volume is 1.2 ~ 1.6mL/g.The character of modified Y zeolite wherein used is as follows: SiO
2/ Al
2o
3mol ratio is 40 ~ 60, and lattice constant is 2.420 ~ 2.450nm, and relative crystallinity is 85% ~ 95%, infrared acidity 0.2 ~ 0.4mmol/g, and wherein the middle strong acid distribution of 300 ~ 500 DEG C is concentrated, and account for 60 ~ 70% of total acid, specific surface area is 500 ~ 1000m
2/ g, pore volume 0.35 ~ 0.55mL/g, wherein the pore volume of the secondary mesopore of 4 ~ 15nm accounts for 35% ~ 55% of total pore volume.The specific surface area of catalyst for hydro-upgrading is 220 ~ 300m
2/ g, pore volume is 0.3 ~ 0.5mL/g, and the pore volume of bore dia 3 ~ 10nm accounts for 80% ~ 95% of total pore volume, and be preferably 85% ~ 95%, infrared acidity is at 0.2 ~ 0.4mmol/g.
In the inventive method, hydro-upgrading reaction zone uses the high-activity hydrogenation modifying catalyst containing amorphous aluminum silicide and modified Y zeolite.Contain in described catalyst for hydro-upgrading: the group VIII metal (with oxide basis) of the modified Y zeolite of 20wt% ~ 60wt% amorphous aluminum silicide, 5wt% ~ 25wt%, the group VIB metal (with oxide basis) of 10wt% ~ 30wt% and 4wt% ~ 10wt%.The character of amorphous aluminum silicide wherein used is as follows: silicon oxide-containing 10wt% ~ 60wt%, and specific surface is 400 ~ 650m
2/ g, pore volume is 1.0 ~ 1.8mL/g, and infrared acidity is 0.34 ~ 0.50mmol/g, and the pore volume that the pore volume of bore dia 4 ~ 10nm accounts for 85% ~ 95%, >15nm of total pore volume accounts for less than 5% of total pore volume; Preferred property is as follows: silicon oxide-containing 10wt% ~ 35wt%, and specific surface is 530 ~ 650m
2/ g, pore volume is 1.2 ~ 1.5mL/g.The character of modified Y zeolite wherein used is as follows: SiO
2/ Al
2o
3mol ratio is 40 ~ 60, and lattice constant is 2.425 ~ 2.440nm, and relative crystallinity is 80% ~ 100%, infrared acidity 0.1 ~ 0.5mmol/g, and wherein the middle strong acid distribution of 250 ~ 550 DEG C is concentrated, and account for 60 ~ 70% of total acid, specific surface area is 600 ~ 900m
2/ g, pore volume 0.3 ~ 0.6mL/g, wherein the pore volume of the secondary mesopore of 4 ~ 15nm accounts for 40% ~ 50% of total pore volume.The components such as aluminum oxide, zirconium white, titanium oxide can also be contained in catalyst for hydro-upgrading.The specific surface area of catalyst for hydro-upgrading is 220 ~ 300m
2/ g, pore volume is 0.3 ~ 0.6mL/g, and the pore volume of bore dia 3 ~ 10nm accounts for 75% ~ 95% of total pore volume, and be preferably 85% ~ 95%, infrared acidity is at 0.3 ~ 0.5mmol/g.
In the inventive method, catalyst for hydro-upgrading A is compared with the composition of catalyst for hydro-upgrading B, group VIB metal in catalyst for hydro-upgrading B and group VIB total metal content 10 ~ 25 percentage ratios, amorphous aluminum silicide in catalyst for hydro-upgrading B and the total content of modified Y zeolite than in catalyst for hydro-upgrading A the two total content low 10 ~ 25 percentage ratios higher than the two total content in catalyst for hydro-upgrading A.
In the inventive method, hydrofinishing reaction zone uses conventional hydrofinishing catalyzer, its active metal component is group vib and group VIII metal, uses procatalyst to carry out prevulcanized, ensures that hydrogenation active metals is in sulphided state in reaction process.Described group vib metal is selected from Mo and/or W, its content with oxide basis for 10 ~ 25%; Group VIII metal is selected from Co and/or Ni, its content with oxide basis for 3 ~ 7%.
In the inventive method, in step (2), the reaction conditions of hydrotreatment reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 250 ~ 420 DEG C, preferably 300 ~ 400 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 1000:1 ~ 1200:1; Volume space velocity 0.1 ~ 1.0h
-1, preferably 0.5 ~ 0.7h
-1.
In the inventive method, in step (3), the reaction conditions of hydro-upgrading reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 250 ~ 370 DEG C, preferably 300 ~ 350 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 800:1 ~ 1000:1; Volume space velocity 0.1 ~ 1.5h
-1, preferably 0.8 ~ 1.0h
-1.
In the inventive method, in step (4), the reaction conditions of hydrofinishing reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 200 ~ 350 DEG C, preferably 290 ~ 320 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 1000:1 ~ 1200:1; Volume space velocity 0.1 ~ 1.5h
-1, preferably 0.8 ~ 1.0h
-1.
Compared with prior art, tool of the present invention has the following advantages:
(1) in the inventive method, catalytic slurry first removes a large amount of sulphur nitrogen by hydrofining reaction on top, hydrotreatment reaction zone, fractional saturation condensed-nuclei aromatics simultaneously, due to hydrofining reaction heat release, make hydrotreatment reaction zone temperature of lower relatively high, due to hydrotreated lube base oil reaction be one not only by thermodynamic effects but also by the reversible reaction of kinetic effect, in the inventive method, by low at bottom, hydrotreatment reaction zone filling vector contg, hydrogenation component content height and hydrogenation activity high, the catalyst for hydro-upgrading A that upgrading activity is low, under the matching effect of catalyst for hydro-upgrading A Hydrogenation and open-loop performance, ensure that condensed-nuclei aromatics hydrotreated lube base oil reaction forward carries out ring-opening reaction while carrying out, the generation of the reversed reaction at utmost avoiding condensed-nuclei aromatics hydrotreated lube base oil to react, and catalyst for hydro-upgrading A open loop activity is low, side chain cleavage reaction can not be there is, make the aromatic hydrocarbons that the number of rings of condensed-nuclei aromatics hydrotreated lube base oil generation belt length side chain is lower, and sulphur nitrogen can be removed further, ensure that liquid is received and object product yield, object product viscosity declines little, to break simultaneously and hindered condensed-nuclei aromatics saturated sterically hindered further, can react under the condition more relaxed for hydro-upgrading reaction zone and create condition.
(2) the inventive method adopts suitable high and low Active hydrogenation modifying catalyst combination, after the open loop of hydro-upgrading reaction zone and hydrofinishing, generate the naphthenic hydrocarbon of a large amount of many side chains of band, can obtain low-temperature performance, with rubber mutual solubility and all good white rubber extending oil base oil of oxidation stability.There is a small amount of straight-chain paraffin isomery of certain influence to become branched paraffin to condensation point simultaneously, ensure the low-temperature performance of product.For the catalytic slurry that added value is lower provides a kind of processing works improving its economy, and develop a kind of new raw material for white rubber extending oil base oil.China is a catalytic slurry resource-rich country, utilize the inventive method can substitute rare naphthenic base crude resource, produce the high-grade white rubber extending oil base oil that rubber industry is badly in need of, effectively can promote the Appropriate application of catalytic slurry resource simultaneously.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the inventive method.
Embodiment
Below in conjunction with accompanying drawing, the inventive method is described in detail.
As shown in Figure 1, enter vacuum still 2 through dehydration and the catalytic slurry 1 that removes mechanical impurity and carry out fractionation, obtain lighting end 3 and last running 4, gained last running 4 can be used as modifying asphalt, heavy fuel oil (HFO), or as coking raw material.Lighting end 3 mixes back end hydrogenation treatment reactor 6 with hydrogen 5; contact with catalyst for hydro-upgrading A with hydrogenation protecting catalyst, Hydrobon catalyst successively; carry out hydrogenation reaction; gained hydrofining effluent 7 enters hydro-upgrading reaction zone 8; in presence of hydrogen, contact with catalyst for hydro-upgrading B, saturated open loop is carried out to two rings and a small amount of thrcylic aromatic hydrocarbon; on rear side of maintenance open loop simultaneously, chain is complete, becomes the monocycle or two Polycyclic aromatic hydrocarbons of being with many side chains.Hydro-upgrading reaction product 9 enters hydrofinishing reaction zone 10, under hydrogen and Hydrobon catalyst exist, carries out aromatic hydrocarbons degree of depth saturated reaction, reduces aromaticity content, ensure the oxidation stability index of product.Then hydrofinishing product 11 enters separation system 12, described separation system 12 generally comprises high-pressure separator and light pressure separator, separating obtained gas phase 13 returns hydrotreating reactor 6 as recycle hydrogen, liquid product 14 obtains gasoline blending component 16, diesel oil blending component 17 and white rubber extending oil base oil product 18 after entering separation column 15 separation.
Below in conjunction with embodiment, the present invention will be further described.
The various catalyzer related in embodiment can select commercial catalyst by character, also can prepare by this area knowledge.The commercial catalysts that the hydrogenation protecting agent of hydroprocessing processes can be selected is as hydrogenation protecting agent such as FZC-100, FZC-102A, FZC-103 of Fushun Petrochemical Research Institute's development and production; The commercial catalysts that can select of Hydrobon catalyst as Fushun Petrochemical Research Institute's development and production 3936,3996, the Hydrobon catalyst such as FF-16, FF-26; The commercial catalysts that hydrofinishing process can be selected is as commodity Hydrobon catalysts such as FV-10, FV-20 of Fushun Petrochemical Research Institute's development and production.
The preparation process of catalyst for hydro-upgrading of the present invention comprises: after amorphous aluminum silicide and modified Y zeolite being mixed, add tackiness agent kneading, roll agglomerating after, extruded moulding on banded extruder and obtain carrier, then load hydrogenation active metals.
The preparation method of amorphous aluminum silicide used, comprises the steps:
A, preparation sodium aluminate solution, sodium silicate solution;
B, by sodium aluminate solution and sodium silicate solution and stream joins in plastic cans, ventilate simultaneously and pass into CO
2gas, adjustment sodium aluminate solution, sodium silicate solution and CO
2flow, controlling material pH value in plastic cans is 9 ~ 11, and controlling neutralization reaction temperature is 20 ~ 50 DEG C, and the neutralization reaction time is 0.5 ~ 1.5 hour;
C, under the control temperature and pH value of step b, said mixture ventilate stablize 0.5 ~ 3.0 hour, be preferably 0.5 ~ 1.0 hour;
D, the solidliquid mixture of step c gained filtered and washs;
E, steps d drying and crushing is obtained amorphous aluminum silicide.
In step a, the concentration of sodium aluminate solution is 25 ~ 60 gAl
2o
3/ L, is preferably 30 ~ 45gAl
2o
3/ L, the concentration of sodium silicate solution is 100 ~ 250gSiO
2/ L, is preferably 100 ~ 150 g SiO
2/ L.
The slurries of steps d gained are filtered and uses 50 ~ 90 DEG C of deionized waters to be washed till neutrality, then 110 ~ 130 DEG C of dryings 6 ~ 8 hours.
PH value in step b is generally constant is 9 ~ 11, is preferably 9.5 ~ 10.5; The neutralization reaction time is generally 0.5 ~ 1.5 hour, is preferably 45 ~ 60 minutes.
In step b, CO
2concentration is 20v% ~ 50v%.Ventilation refers to pass into gas from reaction plastic pot bottom, makes reaction system even, can pass into air or other is not containing CO
2gas.
Amorphous aluminum silicide with sodium aluminate, water glass and carbonic acid gas for prepared by raw material.The method is particularly suitable for the producer adopting sintering process explained hereafter aluminum oxide, with its intermediates sodium aluminate solution and by-product CO
2gas is raw material production amorphous aluminum silicide, the Na produced
2cO
3mother liquor can be circulated to sintering process to provide part Na
2cO
3, form closed cycle, and do not produce contaminated wastewater.
Modified Y zeolite by NaY by the NH of pH value between 1 ~ 3
4 +exchange, hydrothermal treatment consists and acid treatment are prepared from.Concrete preparation process is as follows:
NaY zeolite is by a NH
4nO
3after exchange, and then with oxalic acid and NH
4nO
3mixed solution, carries out second time NH in pH value between 1 ~ 3
4 +exchange, then under 0.080 ~ 0.098 MPa and 500 ~ 550 DEG C condition, carry out first time hydrothermal treatment consists, carry out NH again after hydrothermal treatment consists for the first time
4nO
3exchange, carry out second time hydrothermal treatment consists, second time hydrothermal conditions is 0.1 ~ 0.2MPa and 500 ~ 700 DEG C.Finally use HNO
3carry out acid treatment, obtain modified Y zeolite.
The carrying method of catalyst for hydro-upgrading active metal, can adopt the routine techniques such as kneading method, pickling process to prepare, preferably adopt first extruded moulding, then the mode of impregnating metal component.After the preparation of catalyzer of the present invention adopts modified Y zeolite to mix with contained amorphous silica-alumina dry glue powder, add the appropriate tackiness agent prepared by SB aluminum oxide and nitric acid peptization, kneading or be rolled into paste, extruded moulding, is generally the cylindrical bars of diameter 3 ~ 8 millimeters.Carrier through 100 ~ 130 DEG C of dryings 4 ~ 14 hours, 500 ~ 600 DEG C of roastings 3 ~ 10 hours.After activation, adopt saturated or excessive impregnation fluid containing the steeping fluid of hydrogenation metal, then carry out 100 ~ 130 DEG C of dryings 4 ~ 14 hours, roasting 3 ~ 10 hours at 450 ~ 550 DEG C and make catalyzer.
Particular content and the effect of the inventive method are described below by specific embodiment.
Implementation column below will be further described method provided by the invention, but scope not thereby limiting the invention.The feedstock property of process of the present invention is in table 1.
Table 1 test feedstock property
| Material name | Shandong catalytic slurry |
| Density (20 DEG C), g.cm -3 | 1.0703 |
| Boiling range (simulation distil), DEG C | |
| IBP | 198 |
| 10%/30%/50% | 367/398/421 |
| 70%/90%/95% | 447/475/490 |
| EBP | 511 |
| Sulphur, μ g.g -1 | 4500 |
| Nitrogen, μ g.g -1 | 2074 |
| Carbon residue, % | 3.67 |
| Condensation point, DEG C | 30 |
| Flash-point (opening), DEG C | 112 |
| Mechanical impurity, wt% | 0.047 |
| Mass spectrum forms, wt% | |
| Colloid | 2.9 |
| Paraffinic hydrocarbons | 7.6 |
| Naphthenic hydrocarbon | 36.4 |
| Aromatic hydrocarbons | 53.1 |
| Monocycle/dicyclo/tri-ring | 7.2/5.3/8.7 |
| Fourth Ring/five rings/thiophene | 23.9/0.9/2.3 |
| Do not identify aromatic hydrocarbons | 4.8 |
| Heavy metal, μ g.g -1 | |
| Fe/Ni/V | 12.1/8.12/5.07 |
| Na/Ca | 1.95/4.61 |
Embodiment 1 amorphous aluminum silicide preparation process involved by catalyzer of the present invention below, example 2 is hydro-upgrading catalyst for hydro-upgrading A preparation process, and example 3 is hydro-upgrading catalyst for hydro-upgrading B preparation process.
Embodiment 1
700 solid sodium aluminates being mixed with concentration is 200gAl
2o
3the dense sodium aluminate solution of/L, redilution becomes concentration to be 35gAl
2o
3/ L sodium aluminate working solution (a), gets containing SiO
2the sodium silicate solution of 28wt%, redilution becomes concentration to be 150gSiO
2/ L water glass working solution 2L(b).Get the steel plastic cans of a 30L, open the container valve having (a) and (b) respectively simultaneously, ventilate simultaneously and pass into the CO that concentration is 45v%
2gas, the flow of setting (a) and (b) makes the reaction times at 1 hour, and adjusts CO rapidly
2flow, make the pH of system remain on about 10.0, temperature of reaction 30 DEG C, after (a) and (b) have reacted, stop passing into CO
2, then ventilate and stablize 40 minutes, slurries filter and use 85 DEG C of deionized waters to be washed till neutrality.120 DEG C of dryings 8 hours, pulverize and sieve to obtain amorphous aluminum silicide GL.This amorphous aluminum silicide silicon oxide-containing 30wt%, after activation, specific surface is 560m
2/ g, pore volume is 1.41ml/g, and infrared acidity is 0.42mmol/g, and 90%, the >15nm pore volume that the pore volume of bore dia 4 ~ 10nm accounts for total pore volume accounts for 3% of total pore volume.
Embodiment 2
Get 80g sial GL, 30g modified Y zeolite (SiO
2/ Al
2o
3be 40, lattice constant is 2.432nm, infrared acidity 0.19mmol/g specific surface 866m
2/ g, pore volume 0.52ml/g) tackiness agent be made up of nitric acid and SB alumina peptization with 250g, kneading, rolls, and making can the paste of extrusion, extruded moulding.110 DEG C of dryings 6 hours, 550 DEG C of roastings 4 hours, obtained carrier A.Again with 200ml Mo-Mi co-impregnated solution excessive dipping 80gA2 hour, 110 DEG C of dryings 6 hours, 500 DEG C of roastings 4 hours, obtain catalyst for hydro-upgrading A.Catalyst for hydro-upgrading physical property is in table 2.
Embodiment 3
Get 100g sial GL, 45g modified Y zeolite (SiO
2/ Al
2o
3be 40, lattice constant is 2.432nm, infrared acidity 0.19mmol/g specific surface 866m
2/ g, pore volume 0.52ml/g) tackiness agent be made up of nitric acid and SB alumina peptization with 310g, kneading, rolls, and making can the paste of extrusion, extruded moulding.110 DEG C of dryings 6 hours, 550 DEG C of roastings 4 hours, obtained carrier B.Again with 200ml Mo-Mi co-impregnated solution excessive dipping 80gA2 hour, 110 DEG C of dryings 6 hours, 500 DEG C of roastings 4 hours, obtain catalyst for hydro-upgrading B.Catalyst for hydro-upgrading physical property is in table 2.
Table 2 catalyst for hydro-upgrading physico-chemical property
| Catalyzer is numbered | Catalyst for hydro-upgrading A | Catalyst for hydro-upgrading B |
| MoO 3，wt% | 28.5 | 19.0 |
| NiO，wt% | 10.0 | 6.0 |
| Specific surface area, m 2/g | 241 | 256 |
| Pore volume, ml/g | 0.42 | 0.46 |
| The pore volume of bore dia 3 ~ 10nm accounts for total pore volume, % | 91.0 | 91.4 |
| Infrared total acidity, mmol/g | 0.285 | 0.361 |
Embodiment 4
With Shandong catalytic slurry for raw material, cut point is 500 DEG C, and specific nature is in table 1.The admission space of hydrotreatment reaction zone filling hydrogenation protecting catalyst FZC-103, Hydrobon catalyst 3936 and catalyst for hydro-upgrading A, hydrogenation protecting catalyst FZC-103, Hydrobon catalyst 3936 and catalyst for hydro-upgrading A is than being 1:3:2; Hydro-upgrading reaction zone filling catalyst for hydro-upgrading B; Hydrofinishing reaction zone filling Hydrobon catalyst FV-10, the processing condition of hydrogenation process and product property are in table 3.
Comparative example 1
Adopt the raw material identical with embodiment 1, difference be hydrotreatment products without hydro-upgrading, directly enter hydrofinishing reactor.The admission space of hydrotreatment reaction zone filling hydrogenation protecting catalyst FZC-103, Hydrobon catalyst 3936 and catalyst for hydro-upgrading A, hydrogenation protecting catalyst FZC-103, Hydrobon catalyst 3936 and catalyst for hydro-upgrading A is than being 1:3:2.Hydrofinishing reaction zone filling Hydrobon catalyst FV-10, the processing condition of hydrogenation process and product property are in table 3.
Comparative example 2
Adopt the raw material identical with embodiment 1; difference is that bottom, hydrotreatment reaction zone does not fill catalyst for hydro-upgrading A; hydrotreatment reaction zone filling hydrogenation protecting catalyst FZC-103 and Hydrobon catalyst 3936; the admission space of hydrogenation protecting catalyst FZC-103 and Hydrobon catalyst 3936 is than being 1:5; hydro-upgrading reaction zone filling catalyst for hydro-upgrading B; hydrofinishing reaction zone filling Hydrobon catalyst FV-10, the processing condition of hydrogenation process and product property are in table 3.
The processing condition of table 3 embodiment and comparative example and result
| Test number | Embodiment 4 | Comparative example 1 | Comparative example 2 |
| Hydroprocessing technique condition | |||
| Temperature of reaction, DEG C | 380 | 380 | 390 |
| Reaction pressure, MPa | 15.0 | 15.0 | 15.0 |
| Hydrogen to oil volume ratio | 1000:1 | 1000:1 | 1000:1 |
| Volume space velocity, h -1 | 0.5 | 0.5 | 0.5 |
| Process oily nitrogen content/μ gg -1 | 10 | 10 | 10 |
| Hydro-upgrading reaction process condition | |||
| Temperature of reaction, DEG C | 365 | 375 | |
| Reaction pressure, MPa | 15.0 | 15.0 | |
| Hydrogen to oil volume ratio | 800:1 | 800:1 | |
| Volume space velocity, h -1 | 0.6 | 0.6 | |
| Hydrofinishing reaction process condition | |||
| Temperature of reaction, DEG C | 300 | 310 | 305 |
| Reaction pressure, MPa | 15.0 | 15.0 | 15.0 |
| Hydrogen to oil volume ratio | 800:1 | 800:1 | 800:1 |
| Volume space velocity, h -1 | 0.6 | 0.6 | 0.6 |
| Object product yield, wt% | 59.66 | 65.67 | 55.75 |
| Product property | |||
| Density (20 DEG C), kg.m -3 | 0.8773 | 0.8846 | 0.8814 |
| Viscosity (40 DEG C), mm 2.s -1 | 53.45 | 71.25 | 49.76 |
| Viscosity (100 DEG C), mm 2.s -1 | 6.245 | 8.751 | 5.925 |
| Pour point, DEG C | -24 | 9 | -21 |
| Flash-point (opening), DEG C | 214 | 217 | 212 |
| Refractive power (20 DEG C) | 1.4869 | 1.4945 | 1.4822 |
| Color (D1500), number | <0.5 | <1.0 | <0.5 |
| Saybolt color/number | +30 | +30 | |
| Acid number, mgKOH.g -1 | 0.01 | 0.01 | 0.01 |
| Carbon residue, wt% | 0.01 | 0.01 | 0.03 |
| Ash content, wt% | Vestige | Vestige | Vestige |
| Sulphur content, μ g.g -1 | 1 | 1 | 15 |
| Mass spectrum forms, % | |||
| Naphthenic hydrocarbon | 79.8 | 57.3 | 74.6 |
| One ring naphthenic hydrocarbon/bicyclic ring alkane | 7.0/17.4 | 6.6/11.4 | 6.5/16.2 |
| Tricyclic naphthenes hydrocarbon/Fourth Ring naphthenic hydrocarbon | 19.6/24.3 | 12.5/15.4 | 18.1/20.3 |
| Five rings naphthenic hydrocarbon/six ring naphthenic hydrocarbon | 10.3/3.4 | 7.8/3.6 | 9.5/3.5 |
| Aromatic hydrocarbons | 6.7 | 19.4 | 9.0 |
| Mononuclear aromatics/double ring arene | 3.4/1.0 | 11.6/6.0 | 4.2/1.2 |
| Thrcylic aromatic hydrocarbon/tetra-Polycyclic aromatic hydrocarbons | 0.5/0.2 | 2.3/3.2 | 0.8/0.3 |
| Five rings aromatic hydrocarbons/thiophene | 0.2/0.5 | 2.0/1.7 | 0.3/0.8 |
| Do not identify aromatic hydrocarbons | 0.8 | 2.5 | 1.4 |
| Colloid | 0 | 2.8 | 0 |
Can be found out by the product property of embodiment 4 and comparative example 1, only refine through hydrotreatment and post-refining and do not have hydrogenation modifying process process, products obtained therefrom condensation point is high, and aromaticity content is the highest simultaneously, and oxidation stability, colourity and condensation point are all defective.And in comparison example 2 hydrotreatment reaction zone only fill the scheme product colourity of Hydrobon catalyst, no dress low activity catalyst for hydro-upgrading and condensation point qualified, but object product yield is low, aromaticity content is slightly high simultaneously, and oxidation stability is slightly poor.
Can be found out by the product property in embodiment 4, adopt catalytic slurry can all good color inhibition rubber filling oil base oil of production condensation point, aromaticity content, solvability and oxidation stability by hydrotreatment-hydro-upgrading/hydrogenation post-refining process, gained rubber filling oil performance can meet the performance perameter index of KN4006 white rubber extending oil base oil.Greatly can expand the raw material sources of rubber filling oil base oil, meet the needs of national rubber industry great development, also enrich the deep exploitation of catalytic slurry resource simultaneously, there is very large economic benefit and social benefit.
Claims (13)
1. a catalytic slurry hydrogenation production white rubber extending oil base oil method, comprises following content:
(1) catalytic slurry obtains lighting end and last running through fractionation, and cut point is 480 ~ 510 DEG C;
(2) step (1) described lighting end enters hydrotreatment reaction zone after mixing with hydrogen, contacts successively carry out hydrogenation reaction with hydrogenation protecting catalyst, Hydrobon catalyst with catalyst for hydro-upgrading A;
(3) step (2) gained hydrotreatment effluent enters hydro-upgrading reaction zone, and hydro-upgrading reaction zone uses the catalyst for hydro-upgrading B containing amorphous aluminum silicide and modified Y zeolite, in presence of hydrogen, carries out hydro-upgrading reaction;
(4) step (3) gained hydro-upgrading effluent enters hydrofinishing reaction zone, in presence of hydrogen, with hydrofinishing catalyst exposure, carry out hydrofinishing reaction, hydrofinishing product is isolated to gasoline blending component, diesel oil blending component, white rubber extending oil base oil.
2. in accordance with the method for claim 1, it is characterized in that: step (1) described catalytic slurry carries out fractionation after first carrying out dewatering and remove mechanical impurity again.
3. in accordance with the method for claim 1, it is characterized in that: after the described catalytic slurry fractionation of step (1), gained last running is used as modifying asphalt, heavy fuel oil (HFO), or as coking raw material.
4. in accordance with the method for claim 1; it is characterized in that: hydrotreatment reaction zone loads hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A from top to bottom, the admission space ratio of hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A is 10 ~ 60:20 ~ 70:20 ~ 70.
5. according to the method described in claim 1 or 4; it is characterized in that: hydrotreatment reaction zone loads hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A from top to bottom, the admission space ratio of hydrogenation protecting catalyst, Hydrobon catalyst and catalyst for hydro-upgrading A is 10 ~ 30:45 ~ 60:30 ~ 45.
6. in accordance with the method for claim 1, it is characterized in that: the operational condition of hydrotreatment reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 250 ~ 420 DEG C, preferably 300 ~ 400 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 1000:1 ~ 1200:1; Volume space velocity 0.1 ~ 1.0h
-1, preferably 0.5 ~ 0.7h
-1.
7. the method for right as requested described in 1, is characterized in that: the operational condition of hydro-upgrading reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 250 ~ 370 DEG C, preferably 300 ~ 350 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 800:1 ~ 1000:1; Volume space velocity 0.1 ~ 1.5h
-1, preferably 0.8 ~ 1.0h
-1.
8. the method for right as requested described in 1, is characterized in that: the operational condition of hydrofinishing reaction zone is: reaction pressure 5.0 ~ 20.0MPa, preferably 12.0 ~ 15.0MPa; Temperature of reaction 200 ~ 350 DEG C, preferably 290 ~ 320 DEG C; Hydrogen to oil volume ratio 500:1 ~ 1500:1, preferred 1000:1 ~ 1200:1; Volume space velocity 0.1 ~ 1.5h
-1, preferably 0.8 ~ 1.0h
-1.
9. in accordance with the method for claim 1, it is characterized in that: contain in described catalyst for hydro-upgrading A: the modified Y zeolite of 10wt% ~ 35wt% amorphous aluminum silicide, 2wt% ~ 15wt%, with the group VIII metal of the group VIB metal of oxide basis 20wt% ~ 50wt% and 8wt% ~ 15wt%; Modified Y zeolite containing the amorphous aluminum silicide of 20wt% ~ 60wt%, 5wt% ~ 25wt% in described catalyst for hydro-upgrading B, with the group VIB metal of oxide basis 10wt% ~ 30wt% with the group VIII metal of oxide basis 4wt% ~ 10wt%.
10. in accordance with the method for claim 9, it is characterized in that: catalyst for hydro-upgrading A is compared with the composition of catalyst for hydro-upgrading B, group VIB metal in catalyst for hydro-upgrading B and group VIB total metal content 10 ~ 25 percentage ratios, amorphous aluminum silicide in catalyst for hydro-upgrading B and the total content of modified Y zeolite than in catalyst for hydro-upgrading A the two total content low 10 ~ 25 percentage ratios higher than the two total content in catalyst for hydro-upgrading A.
11. in accordance with the method for claim 9, it is characterized in that: in described catalyst for hydro-upgrading A and catalyst for hydro-upgrading B, the character of amorphous aluminum silicide is as follows: silicon oxide-containing 10wt% ~ 60wt%, and specific surface is 400 ~ 650m
2/ g, pore volume is 1.0 ~ 1.8mL/g, and infrared acidity is 0.34 ~ 0.50mmol/g, and the pore volume that the pore volume of bore dia 4 ~ 10nm accounts for 85% ~ 95%, >15nm of total pore volume accounts for less than 5% of total pore volume.
12. in accordance with the method for claim 9, it is characterized in that: the modified Y zeolite in described catalyst for hydro-upgrading A and catalyst for hydro-upgrading B has following character: SiO
2/ Al
2o
3mol ratio is 40 ~ 60, and lattice constant is 2.425 ~ 2.440nm, and relative crystallinity is 80% ~ 100%, infrared acidity 0.1 ~ 0.5mmol/g, and wherein the middle strong acid distribution of 250 ~ 550 DEG C is concentrated, and account for 60 ~ 70% of total acid, specific surface area is 600 ~ 900m
2/ g, pore volume 0.3 ~ 0.6mL/g, wherein the pore volume of the secondary mesopore of 4 ~ 15nm accounts for 40% ~ 50% of total pore volume.
13. in accordance with the method for claim 1, it is characterized in that: the hydrofinishing catalyzer that hydrofinishing reaction zone uses, its active metal component is group vib and group VIII metal, and described group vib metal is selected from Mo and/or W, its content with oxide basis for 10 ~ 25%; Group VIII metal is selected from Co and/or Ni, its content with oxide basis for 3 ~ 7%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113122324A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for producing special oil product by catalyzing slurry oil hydrogenation |
| CN113122325A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for producing rubber filling oil by catalytic cracking slurry oil |
| CN113122320A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Production method of environment-friendly rubber filling oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331985C (en) * | 2005-09-29 | 2007-08-15 | 中国石油化工集团公司 | Method for producing aromatic hydrocarbon rubber filling oil |
| CN102888243A (en) * | 2012-10-08 | 2013-01-23 | 陕西省能源化工研究院 | Coal tar tail oil fraction and application thereof |
-
2013
- 2013-11-04 CN CN201310532430.3A patent/CN104593067B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331985C (en) * | 2005-09-29 | 2007-08-15 | 中国石油化工集团公司 | Method for producing aromatic hydrocarbon rubber filling oil |
| CN102888243A (en) * | 2012-10-08 | 2013-01-23 | 陕西省能源化工研究院 | Coal tar tail oil fraction and application thereof |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113122324A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for producing special oil product by catalyzing slurry oil hydrogenation |
| CN113122325A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Method for producing rubber filling oil by catalytic cracking slurry oil |
| CN113122320A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Production method of environment-friendly rubber filling oil |
| CN113122320B (en) * | 2019-12-31 | 2023-01-10 | 中国石油化工股份有限公司 | Production method of environment-friendly rubber filling oil |
| CN113122325B (en) * | 2019-12-31 | 2023-01-10 | 中国石油化工股份有限公司 | Method for producing rubber filling oil by catalytic cracking slurry oil |
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