CN104194827A - Hydrorefining treatment process of aromatic hydrocarbon oil - Google Patents
Hydrorefining treatment process of aromatic hydrocarbon oil Download PDFInfo
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- CN104194827A CN104194827A CN201410459927.1A CN201410459927A CN104194827A CN 104194827 A CN104194827 A CN 104194827A CN 201410459927 A CN201410459927 A CN 201410459927A CN 104194827 A CN104194827 A CN 104194827A
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Abstract
The invention relates to a hydrorefining treatment process of aromatic hydrocarbon oil. The hydrorefining treatment process comprises the following steps: mixing the aromatic hydrocarbon oil with hydrogen to obtain a mixture, and feeding the mixture into three fixed bed hydrogenation reactors connected in series in sequence, wherein the process conditions of the fixed bed hydrogenation reactors are as follows: the hydrogen pressure is 5.0-15.0MPa, the temperature is 300-600 DEG C, the hydrogen-oil volume ratio is 300-2000, and the volume space velocity is 0.1h<-1> to 3h<-1>; the fixed bed hydrogenation reactors are a first reactor, a second reactor and a third reactor in sequence, the first reactor is an iron and calcium removal reactor filled with hydrogenation iron and calcium removal catalysts, the second reactor is a demetallization reactor filled with a hydrodemetallization catalyst, and the third reactor is a sulfur and nitrogen removal reactor filled with hydrogenation sulfur and nitrogen removal catalysts. According to the hydrorefining treatment process, a simple hydrogenation treatment process and the proper catalysts are adopted, so that harmful impurities such as sulfur, nitrogen and the like in the aromatic hydrocarbon oil can be effectively removed while the hydrorefining process is carried out, the aromatic hydrocarbon loss is relatively low, the hydrorefined aromatic hydrocarbon oil has the sulfur content of less than 0.5m% and the aromatic hydrocarbon loss is not more than 5m%.
Description
Technical field
The inventive method belongs to chemical technique field, specifically a kind of technique that is applicable to aromatic hydrocarbon oil hydrofining processing.
Technical background
Hydrogen addition technology refers under certain temperature and hydrogen pressure, by the katalysis of catalyzer, stock oil reacted with hydrogen and then improve oil quality or obtain the Technology of target product.
For example gasoline and diesel hydrogenation technology, its objective is and improve petrol and diesel oil quality, reduces the content of objectionable impurities in petrol and diesel oil, reaches Clean Fuel Production, and then reaches the technology of energy-conserving and environment-protective.
Residual hydrogenation is a kind of of mink cell focus hydrogenation, and its object is not only the objectionable impurities of removing in residual oil, makes oil product generation scission reaction under High Temperature High Pressure and catalyst action simultaneously, reaches the object of oil product lighting.
Hydrogenation crude is hydrogen addition technology to be applied to the forefront of oil refining process, makes crude oil obtain refining and part cracking, is the follow-up complete processing condition that facilitates.
In above hydrogen addition technology, to the aromatic hydrocarbons component in oil product, make aromatic ring destroyed as far as possible, generate as far as possible many paraffinic hydrocarbonss, part that can not be destroyed also makes aromatic ring saturated and generate naphthenic hydrocarbon as far as possible.
Aromatic hydrocarbon oil is the optimum feed stock of producing ultra-high power graphite electrode needle coke.Needle coke requires in oil product the content of aromatic hydrocarbons higher in producing, require sulphur in oil product (S) content can not be higher than 0.5m%(weight ratio simultaneously).And prepare the best raw material of aromatic hydrocarbon oil, be catalytic slurry, in catalytic slurry, sulphur content is unstable, and in the crude oil that refinery is processed, the variation of sulphur content directly causes the variation of catalytic slurry dress sulphur content, and then causes the variation of sulphur content in aromatic hydrocarbon oil.Therefore, must take a kind of working method, can higher than the aromatic hydrocarbon oil of 0.5m%, carry out refining desulfurization to sulphur content, make the aromatic hydrocarbons loss in oil product reduce to minimum simultaneously.Under above technical need is impelled, carried out research work of the present invention just.
Summary of the invention
The invention provides a kind of to the hydrorefined Method and process of aromatic hydrocarbon oil, by selecting rightly effective catalyzer, finally reach the object of the objectionable impuritiess such as sulphur (S) in effective elimination aromatic hydrocarbon oil, and in the hydrorefined while, aromatic component in oil product is not destroyed as far as possible, can retains to greatest extent the content of aromatic component.
Technical scheme of the present invention is as follows: aromatic hydrocarbon oil and hydrogen enter three fixed bed hydrogenation reactors of connecting after mixing successively, fixed bed hydrogenation reactor sequentially successively: the first reactor, the second reactor, the 3rd reactor.Wherein the first reactor is deferrization decalcification reactor, and the in-built hydrogen deferrization decalcification catalyzer of dosing of reactor, carries out deferrization decalcification reaction; The second reactor is demetalization reactor, the in-built Hydrodemetalation catalyst of filling out of reactor, Ni, V in main Arene removal oil; The 3rd reactor is desulfurization, denitrification reactor, filling Hydrobon catalyst, hydrodenitrogenation catalyst (the two volume ratio is 8:5), the sulphur in Arene removal oil and nitrogen.
In the present invention, hydrogenation deferrization decalcification catalyzer, Hydrodemetalation catalyst, Hydrobon catalyst and hydrodenitrogenation catalyst, best effect is to reduce gradually in catalyzer aperture from front to back by process sequences, and granularity reduces gradually, and porosity reduces gradually.
In the present invention, load respectively one or more catalyzer in fixed-bed reactor, along logistics direction, catalyzer aperture reduces gradually, and granularity reduces gradually, and porosity reduces gradually.
For effectively improving the ability of imurity-removal, the deferrization decalcification catalyzer using in the present invention is preferably honeycomb shape, order number is between 50～300, generally take porous inorganic oxide as aluminum oxide be carrier, active ingredient is preferably the oxide compound of group VIB metal (as W, Mo) or group VIII metal (as Co, Ni), and the composition of catalyzer is preferably: with AL
2o
3or contain K
2o, MgO, SiO
2, TiO
2aL
2o
3as carrier; Pore volume is 0.1～3.0ml/g, is preferably 0.3～1.3ml/g; Specific surface area is 50～200m
2/ g, is preferably 80～180m
2/ g porosity is 30%～80%, is preferably 35%～65%; Catalyzer, in corresponding burning amount, contains 1%～10%, is preferably 3%～8% group VIB metal (as MoO
3, WO
3) or/and 0.5%～3%, be preferably 1.0%～2.0% group VIII metal (as CoO, NiO).
The Hydrodemetalation catalyst using in the present invention, Hydrobon catalyst, hydrodenitrogenation catalyst generally take porous inorganic oxide as aluminum oxide be carrier, active ingredient is preferably group VIB metal (as W, Mo) or/and the oxide compound of group VIII metal (as Co, Ni), and the composition of catalyzer is preferably: with AL
2o
3or contain K
2o, MgO, SiO
2, TiO
2, ZrO
2aL
2o
3as carrier; Pore volume is 0.1～3.0ml/g, is preferably 0.3～1.3ml/g; Specific surface area is 50～300m
2/ g, is preferably 100～240m
2/ g; Catalyzer, in corresponding burning amount, contains 1%～20%, is preferably 3%～16% group VIB metal (as MoO
3, WO
3) or/and 0.5%～10%, be preferably 3%～6% group VIII metal (as CoO, NiO).
Catalyzer can adopt ordinary method preparation of the prior art (such as the disclosed method of Chinese patent CN101928593A), support of the catalyst in the present invention, its preparation method can be to drip ball forming, spin granulation, extrusion molding, compression molding etc., take a ball forming and extrusion molding as best.Catalyst shape can be honeycombed, spherical, bar shaped, sheet shape, take honeycombed and spherical as best.
In the present invention, the processing condition of fixed bed hydrogenation reactor are: hydrogen pressure 5.0～15.0MPa, is preferably 6.0～12.0MPa; 300～600 ℃ of temperature, are preferably 400～500 ℃; Hydrogen to oil volume ratio 300～2000, is preferably hydrogen to oil volume ratio 400～1500, volume space velocity 0.1h
-1～3h
-1, be preferably 0.2h
-1～1.0h
-1.
The present invention can be used for field of hydrogenation, is particularly useful for aromatic hydrocarbon oil hydrofining and processes, and they are greatly different from conventional hydrogen addition technology, and even target product is completely contradicted.The present invention adopts simple hydrotreatment flow process, select suitable catalyzer, in the hydrorefined while, aromatic component in oil product is not destroyed as far as possible, thereby retains to greatest extent the content of aromatic component, not only can effective elimination aromatic hydrocarbon oil in the detrimental impurity such as sulphur, nitrogen, and aromatic hydrocarbons loss is less, aromatic hydrocarbon oil after desulfurization removing nitric, sulphur content is less than 0.5m%, and aromatic hydrocarbons loss is simultaneously not more than 5m%.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing, method provided by the present invention is further described, but does not therefore limit the present invention.
Referring to Fig. 1, aromatic hydrocarbon oil enters the first reactor (deferrization decalcification reactor) by reactor lower part together with hydrogen, contact and carry out deferrization decalcification reaction with hydrogenation deferrization decalcification catalyzer, its resultant of reaction is without separation, directly autoreactor bottom enters the second reactor (demetalization reactor), contact with Hydrodemetalation catalyst, carry out demetalization (Ni, V) reaction, its resultant of reaction is without separation, directly autoreactor top enters the 3rd reactor (desulfurization removing nitric reactor), with Hydrobon catalyst, hydrodenitrogenation catalyst contact, carry out desulfurization, denitrification reaction.Resultant of reaction enters gas-liquid separation device and carries out gas-liquid separation, and liquid phase part obtains hydrofining aromatic hydrocarbon oil through subsequent disposal again.
Embodiment 1
The present embodiment adopts aromatic hydrocarbon oil hydrofining treatment process of the present invention, stock oil character and 2000 hours reaction results are in Table 1, result by table one is visible, after refinement treatment, the content of sulphur, nitrogen and metallic element is all obviously declined, and sulphur content is less than 0.5m%, and total aromaticity content is only reduced to " 56.6% " by " 59.8% ", loss only be 3.2m%, has reached to expect and be not more than the object of 5m%.
This test is carried out on medium-sized tester, aromatic hydrocarbon oil enters the first reactor (deferrization decalcification reactor) by reactor lower part together with hydrogen, contact and carry out deferrization decalcification reaction with hydrogenation deferrization decalcification catalyzer, its resultant of reaction is without separation, directly autoreactor bottom enters the second reactor (demetalization reactor), contact with Hydrodemetalation catalyst, carry out demetalization (Ni, V) reaction, its resultant of reaction is without separation, directly autoreactor top enters the 3rd reactor (desulfurization removing nitric reactor), with Hydrobon catalyst, hydrodenitrogenation catalyst contact, carry out desulfurization, denitrification reaction.Resultant of reaction enters gas-liquid separation device and carries out gas-liquid separation, and liquid phase part obtains hydrofining aromatic hydrocarbon oil through subsequent disposal again.Wherein deferrization decalcification catalyzer adopts the cellular deferrization decalcifying agent of BN-01A type that Jiangxi Ying Taokangshun Industrial Co., Ltd. produces; Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst are from the buying of Fushun Petrochemical Company catalyst plant, and its preparation method meets embodiment 1,2 preparation methods in CN101928593A.Hydrogenation deferrization decalcification catalyzer, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst additional proportion are respectively: 15%, 20%, 40%, 25%(volume ratio).
This test catalyst physico-chemical property is in Table 2.
This test technology condition is in Table 3.
Table 1 feedstock property forms and test-results
Table 2 catalyzer physico-chemical property
Table 3 processing condition
| Pressure, MPa | 10.0 |
| Hydrogen-oil ratio | 500 |
| Air speed/h -1 | 0.40 |
| Temperature/℃ | 440 |
Claims (9)
1. an aromatic hydrocarbon oil hydrofining treatment process, is characterized in that: aromatic hydrocarbon oil enters three fixed bed hydrogenation reactors of connecting after mixing with hydrogen successively, and the processing condition of described fixed bed hydrogenation reactor are: hydrogen pressure 5.0～15.0MPa; 300～600 ℃ of temperature; Hydrogen to oil volume ratio 300～2000; Volume space velocity 0.1h
-1～3h
-1; Described fixed bed hydrogenation reactor is sequentially successively: the first reactor, the second reactor, the 3rd reactor, and wherein the first reactor is deferrization decalcification reactor, the in-built hydrogen deferrization decalcification catalyzer of dosing of reactor; The second reactor is demetalization reactor, the in-built Hydrodemetalation catalyst of filling out of reactor; The 3rd reactor is desulfurization removing nitric reactor, filling Hydrobon catalyst and hydrodenitrogenation catalyst, the two 8:5 filling by volume, lower floor's filling denitrification catalyst, upper strata filling desulfurization catalyst; Described hydrogenation deferrization decalcification catalyzer is: with AL
2o
3or contain K
2o, MgO, SiO
2, TiO
2, ZrO
2aL
2o
3as carrier; Pore volume is 0.1～3.0ml/g, and specific surface area is 50～200m
2/ g, porosity is 40%～80%; The activeconstituents of catalyzer, in corresponding burning amount, contains 1%～10% group VIB metal or/and 0.5%～3% group VIII metal; Described Hydrodemetalation catalyst and Hydrobon catalyst, hydrodenitrogenation catalyst composition are: with AL
2o
3or contain K
2o, MgO, SiO
2, TiO
2, ZrO
2aL
2o
3as carrier; Pore volume is 0.1～3.0ml/g; Specific surface area is 50～300m
2/ g; Porosity is 30%～80%; The activeconstituents of catalyzer, in corresponding burning amount, contains 1.0%～20.0% group VIB metal or/and 0.5%～8% group VIII metal.
2. aromatic hydrocarbon oil hydrofining treatment process according to claim 1, is characterized in that: described hydrogenation deferrization decalcification catalyzer pore volume is preferably 0.3～1.3ml/g, and specific surface area is preferably 80～180m
2/ g, porosity is preferably 35%～65%; Described catalyst activity composition, in corresponding burning amount, preferably contains 3%～8% group VIB metal or/and 1.0%～2.0% group VIII metal.
3. aromatic hydrocarbon oil hydrofining treatment process according to claim 1 and 2, is characterized in that: the activeconstituents of described hydrogenation deferrization decalcification catalyzer is one or both the oxide compound in Mo, W, and/or one or both the oxide compound in Co, Ni.
4. aromatic hydrocarbon oil hydrofining treatment process according to claim 1, is characterized in that: described Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst pore volume be preferred 0.3～1.3ml/g all, and specific surface area is preferably 100～240m
2/ g; Described catalyst activity composition, in corresponding burning amount, preferably contains 3%～16% group VIB metal or/and 3%～6% group VIII metal.
5. according to the aromatic hydrocarbon oil hydrofining treatment process described in claim 1 or 4, it is characterized in that: the activeconstituents of described Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst is one or both the oxide compound in Mo, W, or/and the oxide compound of one or both in Co, Ni.
6. aromatic hydrocarbon oil hydrofining treatment process according to claim 1, is characterized in that: catalyzer aperture reduces gradually from front to back, granularity reduces gradually, porosity reduces gradually by process sequences for described hydrogenation deferrization decalcification catalyzer, Hydrodemetalation catalyst, Hydrobon catalyst and hydrodenitrogenation catalyst.
7. aromatic hydrocarbon oil hydrofining treatment process according to claim 1, it is characterized in that: in described fixed-bed reactor, load respectively one or more catalyzer, and along logistics direction catalyzer aperture, reduce gradually, granularity reduces gradually, porosity reduces gradually.
8. according to aromatic hydrocarbon oil hydrofining treatment process described in claim 1,2 or 6, it is characterized in that: described deferrization decalcification catalyzer is preferably honeycomb shape, and order number is between 50～300.
9. according to aromatic hydrocarbon oil hydrofining treatment process described in claim 1,2,4,6 or 7, it is characterized in that: the processing condition of described fixed bed hydrogenation reactor are preferably: hydrogen pressure 6.0～12.0MPa; 400～500 ℃ of temperature; Hydrogen to oil volume ratio 400～1500, volume space velocity 0.2h
-1～1.0h
-1.
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Cited By (2)
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| CN105985805A (en) * | 2015-01-29 | 2016-10-05 | 中国石油天然气股份有限公司 | Gradation filling method of heavy oil hydrogenation treatment catalyst |
| CN107794086A (en) * | 2016-09-07 | 2018-03-13 | 中国石油化工股份有限公司 | A kind of hydrocarbons hydrogenation deferrization system and method |
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