CN100335165C - Hydrogenation catalyst, its process and use - Google Patents
Hydrogenation catalyst, its process and use Download PDFInfo
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- CN100335165C CN100335165C CNB200410092428XA CN200410092428A CN100335165C CN 100335165 C CN100335165 C CN 100335165C CN B200410092428X A CNB200410092428X A CN B200410092428XA CN 200410092428 A CN200410092428 A CN 200410092428A CN 100335165 C CN100335165 C CN 100335165C
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Abstract
The present invention relates to a hydrogenation catalyst. The present invention is composed of 10 to 30 wt% of NiO and 70 to 90 wt% of Al2O3. The present invention is produced by that pseudo hydrated alumina powder is dried, steam is induced into the pseudo hydrated alumina powder for reaming, and then, the pseudo hydrated alumina powder is roasted to obtain a macroporous alumina supporter with a large specific surface area; the macroporous alumina supporter with a large specific surface area is immersed in a solution containing nickel compounds, and then, filtering, drying and roasting are carried out to obtain the hydrogenation catalyst. The present invention is suitable for distillate oil containing diene, styrene and derivants thereof; with the hydrogenation catalyst and the production process, hydrogenation can be directly carried out to prepare high-aromatics solvent oil and high-octane petrol.
Description
Technical field
The invention belongs to a kind of hydrogenation catalyst and preparation technology thereof and application, relate in particular to nickel catalyst and technology and application that a kind of alkadienes and styrene and derivative are selected hydrogenation.
Background technology
Pyrolysis gasoline cut fraction is the accessory substance in petroleum hydrocarbon Pintsch process system ethene, the propylene process.Wherein contain alkadienes, styrene, alkynes, indenes equal altitudes unsaturated hydrocarbons, very easily rubber polymerization influences the stable operation of device and catalyst.The task of this catalyst is carried out selective hydrogenation to these unsaturated hydrocarbons exactly, removes alkadienes, styrene and derivative thereof, part alkene and high colloid, improves the stability of product, keeps the aromatic hydrocarbons component simultaneously.
Petroleum chemical enterprise is in order to improve the catalyst cycle of operation, and the drippolene processing technology of employing is: at first with C
5Cut cuts out separately, because C
5The amount the highest (accounting for about 50%) that contains alkadienes in the cut, extremely unstable, easily polymerization.C
5Begin as producing the motor petrol blend component behind fuel or the hydrogenation, or make cracking stock, then be inclined at present and it is isolated one pack system fully utilize.C
6-C
8Cut is then through producing high-quality solvent naphtha or production benzene,toluene,xylene aromatic hydrocarbons behind the two-stage hydrogenation.C
9And above fraction is then because of its component complexity, and heavy ends are many, and colloid and sulfur content height are very unstable, and typical catalyst is difficult to handle, and generally also it is isolated, and is mainly used in and produces aromatic hydrocarbons Petropols and high aromatic solvent naphtha.
Along with improving constantly of ethene and propone output, drippolene and C
9And the quantity of above fraction increases year by year, because the raising of environmental requirement, the consumption of aromatic hydrocarbons Petropols is limited, therefore develops C
9And above fraction is significant.
U.S. Pat 20020002315 has specifically described a kind of diolefin hydrogenate technology, catalyst be the 5-15% Ni on aluminium oxide, or 3-6% nickel oxide and 12-25% molybdenum oxide are carried on the aluminium oxide simultaneously.Raw material can be C
5-C
15Cut, sulfur content can be up to 0.2%, and catalyst does not need activation or preconditioning before use.Reaction temperature is 150-300 ℃, and pressure is 300-600psig (being about 2.0-4.0MPa), and air speed is 2-15h
-1, H
2Flow is 100-1000SCF/B, (is equivalent to H
2/ Oil=30-300 (V/V)).This technology can remove 80-90% with alkadienes.The shortcoming of this technology is: reaction temperature is higher, and under this temperature, alkadienes self is polymerization easily just, is unfavorable for the catalyst long-term operation.5-15%Ni/Al in this patent
2O
3Catalyst, the cycle of operation is 70 days first, 3-6%NiO and 12-25%MoO
3/ Al
2O
3Catalyst, the cycle of operation is 23 days first.
A kind of selection hydrogenation catalyst of invention such as Research Inst. of Petroleum Processing, SINOPEC Sun Lian rosy clouds, the patent No. is ZL97121810.This catalyst is by the nickel oxide of 5-25%, and the aluminium oxide of the lithium of 0.1-2.0% or alkaline-earth metal and surplus is formed.This catalyst is applicable to the selection hydrogenation of the full distillate oil of drippolene, and application conditions is reaction temperature 75-140 ℃, pressure 2.7MPa, liquid volume air speed 2.1h
-1, H
2/ Oil=188 (V/V), the product diene value is at 2-3.The shortcoming of this catalyst is that auxiliary agent lithium price is expensive, and the preparation process complexity of catalyst carrier needs to carry out hydrothermal treatment consists with the water of 1.3-2.5MPa, or in roasting more than 900 ℃, equipment required height, and the lower (60-90m of the specific surface of catalyst
2/ g), the less relatively (0.29-0.36cm of pore volume
3/ g), reactivity is relatively low.
And above-mentioned two patents all do not have to describe to the styrene of very easily polymerization and the hydrogenation of derivative.
Summary of the invention
The purpose of this invention is to provide catalyst and the technology and the application of alkadienes and the styrene and the derivative selection hydrogenation of a kind of high activity, life-span length.
Catalyst weight percentage of the present invention consists of:
NiO：10-30％，Al
2O
3：70-90％。
Catalyst of the present invention has high-ratio surface and large pore volume and large aperture, and specific area is 100-200m
2/ g, pore volume are 0.35-0.85cm
3/ g, the pore volume that has greater than the hole of 5nm accounts for the 85%-95% of total pore volume, and its most probable aperture is in the 10-20nm scope.
Preparation of catalysts method of the present invention is as follows:
(1) intends thin pigment system globulate, strip or plate shape with the aluminium hydroxide of salic 60-80wt%, after under 80-120 ℃ dry 3-8 hour, in atmospheric air, temperature is risen to 600-700 ℃, constant temperature 1-4 hour, feed water vapour, the volume ratio of steam and air is 20-80%, again constant temperature 1-4 hour with this understanding, stop water vapour then, 600-700 ℃ is continued roasting 2-4 hour down in air, obtain high-ratio surface, the alumina catalyst support of macropore;
(2) consist of by catalyst weight percentage: NiO:10-30%, Al
2O
3: 70-90%, adopt infusion process with alumina support, according to the composition of catalyst, with the nickel compound solution impregnation of nickeliferous 120-230 grams per liter concentration 3-6 hour, filter, dipping is back to be descended dry 8-15 hour at 80-120 ℃, made catalyst at 350-500 ℃ of roasting 3-5 hour.
The shape that aforesaid aluminium hydroxide is intended thin pigment body is preferably spherical.
The preferred nickel nitrate of aforesaid nickel compound.
Catalyst of the present invention is applied to C
5-C
10Feedstock oil in the hydrogenation of alkadienes and styrene and derivative thereof, reaction process condition is: temperature: 50-200 ℃, pressure: 2.0-4.0MPa, liquid air speed LHSV=1-10h
-1, hydrogen to oil volume ratio is: H
2/ oil=100-300.
Aforesaid C
5-C
10Feedstock oil can be proportion 0.80-0.89cm
3/ g, boiling range 35-230 ℃ gasoline fraction, wherein diene value is at 4-40gI/100g, and bromine number is at 20-95gBr/100g, and styrene and derivative content are at 1-30wt%, and actual gum content is 5-200mg/100ml, sulfur content＜300ppm.
The present invention is characterized in that compared with prior art this catalyst has high surface area, helps the high degree of dispersion of active constituent, and the pore volume and the aperture of catalyst are all bigger simultaneously, help improving hydrogenation activity and anticol mass-energy power.Thereby this catalyst is active higher than present existing similar catalyst, and the service cycle of catalyst is long, and preparation technology is simple, good economy performance.Be embodied in:
1. activity of such catalysts and anticol mass-energy Z-TEK are not good.Can be with C
9And styrene and the derivative of the middle 15-25% of above heavy component (boiling range: 80-230 ℃), hydro-conversion is more than 95% under lower reaction temperature (80-150 ℃).When adopting full-cut fraction pyrolysis gasoline (boiling range: 35-205 ℃), catalyst operation 100 days, the result is still more stable, and the product diene value is less than 1.
2. catalyst is strong to adaptability to raw material, can be to the full cut (C of drippolene
5-C
10) directly carry out hydrogenation, needn't isolate C
5And C
9, and to the heavy component (C of good utilisation not of general petroleum chemical enterprise
9And above component) also hydrogenation be can directly carry out, high-knock rating gasoline and high aromatic solvent naphtha produced.Raw material can be proportion 0.80-0.89cm
3/ g, boiling range 35-230 ℃ gasoline fraction, wherein diene value is at 4-40gI/100g, and bromine number is at 20-95gBr/100g, and styrene and derivative content are at 1-30%, and actual gum content is 5-200mg/100ml, sulfur content＜300ppm.
The specific embodiment
Further specify the present invention below by example, but the present invention is not restricted to this.
Embodiment 1:
The thin water-aluminum hydroxide powder of plan with salic 62wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 120 ℃ dry 3 hours, in atmospheric air, temperature is risen to 600 ℃, constant temperature 2 hours, feed water vapour, the volume ratio of steam and air is 50%, with this understanding constant temperature 2 hours again, stop water vapour then, 600 ℃ are continued roasting 3 hours in air.The nickel nitrate solution dipping that adopts nickeliferous 120 grams per liter concentration filtered after 3 hours, and drying is 15 hours under 80-90 ℃, and 480 ℃ of roastings 4 hours.Again repeated impregnations once, reaching required high nickel content, dry and roasting condition is the same.
The catalyst of preparation consists of: NiO:28.5%, Al
2O
3: 71.5%.Specific area: 180 meters
2/ gram, pore volume: 0.46 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 90% of total pore volume, and its most probable aperture is at 11nm.
Catalyst performance evaluation: raw materials used oil nature sees Table 1.In fixed bed reactors, pack into the catalyst of 50ml.At reaction pressure 3.0MPa, feed liquid air speed 5.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 250, under reaction temperature 80-150 ℃ the condition, catalyst operation 105 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 98%.
Embodiment 2:
The thin water-aluminum hydroxide powder of plan with salic 70wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 110 ℃ dry 4 hours, in atmospheric air, temperature is risen to 630 ℃, constant temperature 1 hour, feed water vapour, the volume ratio of steam and air is 80%, with this understanding constant temperature 2 hours again, stop water vapour then, 650 ℃ are continued roasting 2 hours in air.Adopt the nickel nitrate solution of nickeliferous 130 grams per liter concentration, flood after 4 hours and filter, drying is 10 hours under 90-100 ℃, and 350 ℃ of roastings 5 hours.
The catalyst of preparation consists of: NiO:19.6%, Al
2O
3: 80.4%.Specific area: 150 meters
2/ gram, pore volume: 0.65 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 93% of total pore volume, and its most probable aperture is at 15nm.
Catalyst performance evaluation: raw materials used oil nature sees Table 1.In fixed bed reactors, pack into the catalyst of 50ml.At reaction pressure 3.0MPa, feed liquid air speed 3.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 200, under reaction temperature 100-150 ℃ the condition, catalyst operation 120 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 98%.
Embodiment 3:
The thin water-aluminum hydroxide powder of plan with salic 75wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 100 ℃ dry 5 hours, in atmospheric air, temperature is risen to 660 ℃, constant temperature 1 hour, feed water vapour, the volume ratio of steam and air is 30%, with this understanding constant temperature 2 hours again, stop water vapour then, 680 ℃ are continued roasting 2 hours in air.Adopt the nickel nitrate solution of nickeliferous 150 grams per liter concentration, flood after 5 hours and filter, drying is 8 hours under 110-120 ℃, and 400 ℃ of roastings 3 hours.
The catalyst of preparation consists of: NiO:12.5%, Al
2O
3: 87.5%.Specific area: 110 meters
2/ gram, pore volume: 0.82 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 95% of total pore volume, and its most probable aperture is at 19nm.
Catalyst performance evaluation: raw materials used oil is the heavy component that drippolene cuts out, and character sees Table 2.In fixed bed reactors, pack into the catalyst of 50ml.At reaction pressure 4.0MPa, feed liquid air speed 2.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 150, under reaction temperature 120-150 ℃ the condition, catalyst operation 120 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 96%.
Embodiment 4:
The thin water-aluminum hydroxide powder of plan with salic 78wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 90 ℃ dry 6 hours, in atmospheric air, temperature is risen to 600 ℃, constant temperature 2 hours, feed water vapour, the volume ratio of steam and air is 20%, with this understanding constant temperature 2 hours again, stop water vapour then, 620 ℃ are continued roasting 3 hours in air.Adopt the nickel nitrate solution of nickeliferous 180 grams per liter concentration, flood after 6 hours and filter, drying is 10 hours under 120 ℃, and 500 ℃ of roastings 4 hours.Again repeated impregnations once, reaching required high nickel content, dry and roasting condition is the same.
The catalyst of preparation consists of: NiO:24.5%, Al
2O
3: 75.4%.Specific area: 190 meters
2/ gram, pore volume: 0.56 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 85% of total pore volume, and its most probable aperture is at 12nm.
Catalyst performance evaluation: raw materials used oil nature sees Table 2.In fixed bed reactors, pack into the catalyst of 50ml.At reaction pressure 3.0MPa, feed liquid air speed 5.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 220, under reaction temperature 70-150 ℃ the condition, catalyst operation 105 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 98%.
Embodiment 5:
The thin water-aluminum hydroxide powder of plan with salic 70wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 80 ℃ dry 8 hours, in atmospheric air, temperature is risen to 680 ℃, constant temperature 1 hour, feed water vapour, the volume ratio of steam and air is 50%, with this understanding constant temperature 2 hours again, stop water vapour then, 680 ℃ are continued roasting 2 hours in air.Adopt the nickel nitrate solution of nickeliferous 200 grams per liter concentration, flood after 3.5 hours and filter, drying is 10 hours under 90 ℃, and 450 ℃ of roastings 4 hours.
The catalyst of preparation consists of: NiO:15.5%, Al
2O
3: 84.5%.Specific area: 105 meters
2/ gram, pore volume: 0.75 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 94% of total pore volume, and its most probable aperture is at 20nm.
Catalyst performance evaluation: raw materials used oil is full fraction drippolene, and character sees Table 3.In fixed bed reactors, pack into the catalyst of 25ml.At reaction pressure 3.0MPa, feed liquid air speed 4.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 250, under reaction temperature 80-150 ℃ the condition, catalyst operation 140 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 99%.
Embodiment 6:
The thin water-aluminum hydroxide powder of plan with salic 66wt% (all the other are water) is made the bead that diameter is 2-5mm, after under 120 ℃ dry 3.5 hours, in atmospheric air, temperature is risen to 620 ℃, constant temperature 1 hour, feed water vapour, the volume ratio of steam and air is 80%, with this understanding constant temperature 3 hours again, stop water vapour then, 640 ℃ are continued roasting 2 hours in air.Adopt the nickel nitrate solution of nickeliferous 230 grams per liter concentration, flood after 4.5 hours and filter, drying is 12 hours under 110 ℃, and 480 ℃ of roastings 4 hours.
The catalyst of preparation consists of: NiO:10.5%, Al
2O
3: 89.5%.Specific area: 160 meters
2/ gram, pore volume: 0.64 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 92% of total pore volume, and its most probable aperture is at 16nm.
Catalyst performance evaluation: raw materials used oil is full fraction drippolene, and character sees Table 3.In fixed bed reactors, pack into the catalyst of 25ml.At reaction pressure 3.0MPa, feed liquid air speed 2.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 180, under reaction temperature 90-150 ℃ the condition, catalyst operation 105 days, its result is still more stable, and the product diene value is less than 1, styrene conversion rate 97%.
Comparative Examples
Catalyst consists of: NiO:10.2%, Al
2O
3: 89.8%.Specific area: 60 meters
2/ gram, pore volume: 0.26 milliliter/gram, the pore volume that has greater than the hole of 5nm accounts for 94% of total pore volume, and its most probable aperture is at 17nm.
Catalyst performance evaluation: raw materials used oil is full fraction drippolene, and character sees Table 3.In fixed bed reactors, pack into the catalyst of 25ml.At reaction pressure 3.0MPa, feed liquid air speed 2.0h
-1, hydrogen to oil volume ratio H
2Under/oil=condition of 180, under reaction temperature 120-170 ℃ the condition, the catalyst operation is after 65 days, and the product diene value is just greater than 1, styrene conversion rate 93%.
Table 1. drippolene component character
| Density | Gram per centimeter 3 | 0.84-0.85 |
| Existent gum | Milligram/100 centimetres 3 | 60-100 |
| Diene value | Gram iodine/100 grams | 15-25 |
| Styrene and derivative thereof | wt％ | 5-10 |
| The bromine valency | Gram bromine/100 grams | 60-70 |
| Sulphur | ppm | 80-110 |
| Boiling range | ℃ | |
| Fore-running | 55 | |
| 10％ | 70 | |
| 50％ | 110 | |
| 90％ | 175 | |
| Do | 198 |
Table 2.C
9And above drippolene heavy component character
| Density | Gram per centimeter 3 | 0.88-0.89 |
| Existent gum | Milligram/100 centimetres 3 | 150-180 |
| Diene value | Gram iodine/100 grams | 5-10 |
| Styrene and derivative thereof | wt％ | 15-20 |
| The bromine valency | Gram bromine/100 grams | 45-55 |
| Sulphur | ppm | 150-180 |
| Boiling range | ℃ | |
| Fore-running | 90 | |
| 10％ | 142 | |
| 50％ | 165 | |
| 90％ | 195 | |
| Do | 210 |
Table 3. full-cut fraction pyrolysis gasoline component character
| Density | Gram per centimeter 3 | 0.81-0.83 |
| Existent gum | Milligram/100 centimetres 3 | 20-50 |
| Diene value | Gram iodine/100 grams | 25-35 |
| Styrene and derivative thereof | wt％ | 2-3 |
| The bromine valency | Gram bromine/100 grams | 68-80 |
| Sulphur | ppm | 60-70 |
| Boiling range | ℃ | |
| Fore-running | 33 | |
| 10％ | 55 | |
| 50％ | 105 | |
| 90％ | 164 | |
| Do | 188 |
Claims (6)
1, a kind of hydrogenation catalyst is characterized in that catalyst weight percentage consists of:
NiO：10-30％，Al
2O
3：70-90％；
Described hydrogenation catalyst specific area is 100-200m
2/ g, pore volume are 0.35-0.85cm
3/ g, the pore volume that has greater than the hole of 5nm accounts for the 85%-95% of total pore volume, and its most probable aperture is in the 10-20nm scope.
2, the preparation technology of the described hydrogenation catalyst of a kind of claim 1 is characterized in that comprising the steps:
(1) intends thin pigment system globulate, strip or plate shape with the aluminium hydroxide of salic 60-80wt%, after under 80-120 ℃ dry 3-8 hour, in atmospheric air, temperature is risen to 600-700 ℃, constant temperature 1-4 hour, feed water vapour, the volume ratio of steam and air is 20-80%, again constant temperature 1-4 hour with this understanding, stop water vapour then, 600-700 ℃ is continued roasting 2-4 hour down in air, obtain high-ratio surface, the alumina catalyst support of macropore;
(2) consist of by catalyst weight percentage: NiO:10-30%, Al
2O
3: 70-90%, adopt infusion process with alumina support, according to the composition of catalyst, with the nickel compound solution impregnation of nickeliferous 120-230 grams per liter concentration 3-6 hour, filter, dipping is back to be descended dry 8-15 hour at 80-120 ℃, made catalyst at 350-500 ℃ of roasting 3-5 hour.
3, a kind of hydrogenation catalyst preparation technology as claimed in claim 2 is characterized in that described aluminium hydroxide plan approaches the sphere that is shaped as of pigment body.
4, a kind of hydrogenation catalyst preparation technology as claimed in claim 2 is characterized in that described nickel compound is a nickel nitrate.
5, the application of the described hydrogenation catalyst of a kind of claim 1 is characterized in that catalyst is applied to C
5-C
10Feedstock oil in the hydrogenation of alkadienes and styrene and derivative thereof, reaction process condition is: temperature: 50-200 ℃, pressure: 2.0-4.0MPa, the liquid air speed is 1-10h
-1, hydrogen to oil volume ratio is: H
2/ oil=100-300.
6, the application of a kind of hydrogenation catalyst as claimed in claim 5 is characterized in that described C
5-C
10Feedstock oil be proportion 0.80-0.89cm
3/ g, boiling range 35-230 ℃ gasoline fraction, wherein diene value is at 4-40gI/100g, and bromine number is at 20-95gBr/100g, and styrene and derivative content thereof are at 1-30wt%, and actual gum content is 5-200mg/100ml, sulfur content＜300ppm.
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|---|---|
| CN1644656A (en) | 2005-07-27 |
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Assignee: Karamay Konka Chemical Co., Ltd. Assignor: Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences Contract record no.: 2010650000004 Denomination of invention: Hydrogenation catalyst, its process and use Granted publication date: 20070905 License type: Exclusive License Open date: 20050727 Record date: 20100527 |