CN102399588A - Method for reducing sulfur content in sulfur-containing light oil - Google Patents
Method for reducing sulfur content in sulfur-containing light oil Download PDFInfo
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Abstract
The invention relates to a method used for reducing the sulfur content in sulfur-containing light oil. The method comprises steps that: a light oil raw material is delivered into a primary hydrodesulfurization processing reactor, and is subject to contact reaction with a hydrodesulfurization catalyst C1; an effluent is delivered into a secondary hydrodesulfurization processing reactor, and is subject to contact reaction with a hydrodesulfurization catalyst C2; an effluent is processed through gas-liquid separation, such that a light oil product with low sulfur content is obtained. According to the invention, a fixed bed reactor structure is adopted in both the primary hydrodesulfurization processing reactor and the secondary hydrodesulfurization processing reactor. The two stages of hydrodesulfurization processing reactors are connected in series. The sulfur-containing light oil is processed through two times of continuous hydrodesulfurization reactions, such that sulfur content is reduced. Hydrodesulfurization is ensured, an alkene reducing phenomenon can be effectively controlled, loss of octane number can be controlled, and the reaction conditions are mild. The hydrogenation-modified light oil product provided by the invention is not required to be processed through alkali washing, the octane number loss of the product is low, and a yield of the product is higher than 99%.
Description
Technical field
The present invention relates to a kind of method of light oil upgrading, more particularly, relate to sulphur content in a kind of reduction light oil, produce the post-treating method of low-sulfur or super low-sulfur oil blend component.
Background technology
Along with developing rapidly of automotive industry, the atmospheric pollution that vehicle exhaust causes is particularly serious, and contained sulfide and alkene is the main precursor that produces noxious emission in the gasoline.Catalytically cracked gasoline, the sulfide in petrol that is particularly obtained by heavy oil and RCC and the content of alkene are high, are the main sources of sulfur in gasoline and alkene.The sulfocompound in the catalytically cracked gasoline and the characteristic distributions of alkene are: sulfide mainly concentrates in the last running (HCN), and the sulfide in the lighting end (LCN) is main with mercaptan; Olefin(e) centent in the lighting end is higher than the olefin(e) centent in the last running, and high-octane olefin component concentrates in the lighting end.Therefore, at present both at home and abroad hydrodesulfurization mainly adopt the segmentation cutting process method (like Prime-G, Prime-G+; RSDS-I, RSDS-II), in hydrodesulfurization; Earlier the heavy fractioning hydrogenation desulfurization is handled; Mix with lighting end then, avoided the saturated in a large number of alkene in the sweetening process, reduced the loss of octane value.
CN102061194A discloses a kind of method that reduces content of sulfur in gasoline, and this method comprises two-stage reaction, and gasoline stocks at first is fractionated into light gasoline fraction, middle gasoline fraction and heavy naphtha; Light gasoline fraction carries out getting into the product jar behind the mercaptan removal; In gasoline fraction and heavy naphtha get into first hydrotreating reactor respectively and second hydrotreating reactor carries out the selective hydrodesulfurization reaction, two reactor outlet materials mix after after the cooling, separation, fractionation, entering product jar.Wherein, carrier of hydrogenating catalyst is selected from unformed aluminum oxide or silica-alumina supports, and active metal component is molybdenum and/or tungsten, nickel and/or cobalt.Reaction conditions is 200～490 ℃ of temperature of reaction, reaction pressure 1.0～4.0MPa, volume space velocity 2～8.0h
-1, hydrogen to oil volume ratio 200～1000Nm
3/ m
3
CN1458235A introduces a kind of octane value recovering catalyst and methods for making and using same thereof; Be characterized in; Be light, last running with the fractionation of full cut catalytic gasoline earlier; Under conventional hydrogen refining process condition, remove the sulfide in the last running, then catalytic gasoline last running desulfurization product is passed through octane value recovering catalyst, the loss of octane number that the last running of compensation catalytic gasoline causes because of hydrogenating desulfurization.Octane value recovering catalyst is a staple with nickel oxide/ZSM-5+Beta, and wherein nickel oxide content is 1m%～10m%, and ZSM-5+Beta content is 50m%～89m%, alumina binder 10m%～45m%.Reaction conditions is: reaction pressure 1.0MPa～4.0MPa, 340 ℃～440 ℃ of temperature of reaction, volume space velocity 1.0h
-1～5.0h
-1With hydrogen to oil volume ratio 200～800: 1.
CN1796502A discloses a kind of gasoline modifying method; This technology is two sections tandem process; At first gasoline fraction oil is contacted with a kind of olefin isomerization catalyst, the catalytic gasoline isomerization product is contacted with a kind of Hydrobon catalyst carry out hydrodesulfurization reaction then.Wherein said olefin skeletal isomerization catalyzer is combined by catalyst I and catalyst I I, and its loss of octane number of gasoline fraction through this method upgrading is greater than 2.0,
CN1339564A discloses a kind of method of carrying out upgrading through three sections reaction pair gasoline; This method comprises three sections reactions; Gasoline carries out diolefin selective hydrogenation at first section earlier, gets into second section then and carries out olefin isomerization, gets into the 3rd section at last and carries out hydrogenation reaction.Second section olefin isomerization wherein, catalyzer is selected from Al
2O
3, halogen-containing Al
2O
3, SAPO-11, ZSM-12, ZSM-22, MCM-22, MCM-41 one or several, reaction conditions is 100 ℃～500 ℃ of temperature of reaction, reaction pressure 0.1MPa～4.0MPa, gasoline weight space velocity 0.1～10h
-1
U.S.Pat.No.5,362,376 have introduced two sections assembly catalyze desulfurization process of gasoline of a kind of hydrogenating desulfurization/octane value recovering.This technology is cut into light gasoline fraction and heavy naphtha with gasoline stocks earlier; Catalytic gasoline last running is at first carried out desulfurization through a kind of conventional hydrogenating desulfurization Mo-Co or Mo-Ni catalyzer; Desulfurization product is handled through the mesopore HZSM-5 zeolite catalyst that contains nickel oxide more then; Low-octane alkane is selected the type cracking or isomery turns to high-octane hydro carbons, thereby recover because of the saturated loss of octane number that causes of hydrogenation of olefins in the hydrodesulfurization process.The pellet density of this patent catalyst system therefor is that 0.98g/ml, specific surface area are 336m
2/ g, pore volume are that 0.65ml/g, average pore diameter are 7.7nm.
U.S.Pat.No.5,413,696 have introduced two sections assembly catalyze gasoline desulfurs of a kind of hydrogenating desulfurization/octane value recovering novel process.Be characterized in that catalytic gasoline last running at first carries out desulfurization through a kind of conventional hydrogenating desulfurization Mo-Co or Mo-Ni catalyzer; Desulfurization product is handled through the macropore HBeta zeolite catalyst that contains nickel oxide more then; Low-octane alkane is selected the type cracking or isomery turns to high-octane hydro carbons, thereby recover because of the saturated loss of octane number that causes of alkene in the hydrodesulfurization process.
U.S.Pat.No.5,413,698 have introduced two sections assembly catalyze gasoline desulfurs of a kind of hydrogenating desulfurization/octane value recovering novel process.The same U.S.Pat.No.5 of this technology, 362,376 and U.S.Pat.No.5; 413; 696 technologies are similar, at first catalytic gasoline last running carried out desulfurization through a kind of conventional hydrogenating desulfurization Mo-Co or Mo-Ni catalyzer, and desulfurization product is handled through the mesopore HZSM-5 zeolite/macropore HBeta zeolite catalyst that contains nickel oxide more then; Low-octane alkane selective cracking or isomery are turned to high-octane hydro carbons, thereby recover because of the saturated loss of octane number that causes of hydrogenation of olefins in the hydrodesulfurization process.
EP0940464 discloses a kind of process method of catalytically cracked gasoline desulfurization.With catalytic gasoline of whole fraction cut into gently, in, weigh three sections cuts, with the heavy fractioning hydrogenation desulfurization, with the cooling of first bed outlet elute, be mixed into the second bed hydrogenating desulfurization at first bed then with middle runnings.This method first bed temperature of reaction is 360 ℃, and alkene is all saturated, 302 ℃ of the second bed temperature of reaction, and the alkene saturation exponent is 57%, and the alkene saturation exponent is high in this method hydrogenation process, and loss of octane number is big.
Above-mentioned disclosed method all is mainly to concentrate on lighting end according to olefin(e) centent in the gasoline; And sulphur mainly concentrates on the characteristics of last running; Earlier with light oil be cut into gently, last running or gently, in, last running, last running is carried out mixing with lighting end after the hydrogenating desulfurization, obtains clean gasoline.Not only technology is loaded down with trivial details for aforesaid method, energy consumption is high, and the alkene saturation exponent of light oil is high in the treating processes, the loss of octane value is big.
Summary of the invention
The objective of the invention is to full cut and all suitable hydrodesulfurization of last running sour crudes; The existing shortcoming that technology is loaded down with trivial details and energy consumption is high of upgrading; A kind of method of new reduction light oil sulfur content is provided; Can reach set objective according to oil product characteristics and production demand modulation processing condition, in removing light oil, can effectively control the saturated little purpose of loss of octane number that reaches of alkene during sulfide.Specifically may further comprise the steps:
1. the light oil raw material gets into one-level hydrogenating desulfurization treatment reactor, with Hydrobon catalyst C1 contact reacts;
2. the elute that 1. reacts of step gets into the secondary hydrodesulphurisatioreactors reactors, with Hydrobon catalyst C2 contact reacts;
3. the elute that 2. reacts of step obtains the low light oil products of sulphur content after separating;
Said one-level hydrogenating desulfurization treatment reactor and secondary hydrogenating desulfurization treatment reactor all adopt the fixed-bed reactor structure;
Said Hydrobon catalyst C1 is group vib base metal and the group VIII non-precious metal catalyst that loads on the complex carrier.
Said Hydrobon catalyst C2 carrier is zirconium white, titanium oxide, aluminium oxide-titanium oxide, aluminium oxide-zirconium oxide, and active ingredient is nickel and/or cobalt.
The hydrogen rich gas that 3. step obtains after the gas-liquid separation removes hydrogen sulfide, and with after fresh hydrogen is mixed, and a part is mixed with raw oil and carried out hydrodesulfurization reaction, and another part is as the cold hydrogen of one-level hydrogenating desulfurization treatment reactor and secondary hydrogenating desulfurization treatment reactor.
The liquid efflunent that 3. step obtains after the gas-liquid separation is handled top, back elute entering return tank through stabilizer tower and is isolated dry gas (staple is C
1～C
2Hydro carbons), remaining liquid is back to stabilizer tower through overhead condenser.
The liquid efflunent that 3. step obtains after the gas-liquid separation is circulated to stabilizer tower handle the part entering tower bottom reboiler of bottom, back elute through stabilizer tower after, and another part is the light oil products of low sulfur content.
Said one-level hydrogenating desulfurization treatment reactor reaction conditions: hydrogen partial pressure 1.0～3.0MPa, 250～350 ℃ of temperature of reaction, volume space velocity 1.0～4.0h
-1, hydrogen to oil volume ratio 200～700ml/ml.
Said secondary hydrogenating desulfurization treatment reactor reaction conditions: hydrogen partial pressure 1.0～3.0MPa, 250～380 ℃ of temperature of reaction, volume space velocity 2.0～6.0h
-1, hydrogen to oil volume ratio 200～700ml/ml.
Said light oil raw material is one or more in catalytically cracked gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, steam cracking gasoline, the pyrolysis gasoline.
Among the present invention, the complex carrier of said Hydrobon catalyst C1 is the complex carrier of aluminum oxide and molecular sieve, perhaps is the complex carrier of amorphous silicon aluminium and molecular sieve.
Said molecular sieve is preferably the ZSM-5 molecular sieve; Said complex carrier is preferably the complex carrier of aluminum oxide and ZSM-5.
Said group vib base metal is molybdenum and/or tungsten, is benchmark with complex carrier weight, and the content of described molybdenum and/or tungsten is 5.0～15.0%.
Said group VIII base metal is nickel and/or cobalt, is benchmark with the vehicle weight, and the content of nickel and/or cobalt is 0.5～6.0%.
The method preparation that the concrete preparation method of above-mentioned catalyzer C1 provides by the patent of publication number CN102051208A.
Among the present invention, said Hydrobon catalyst C2 is a benchmark with the vehicle weight, and the content of nickel and/or cobalt is 1.0～20.0%.
The method preparation that the concrete preparation method of above-mentioned catalyzer C2 provides by the patent of publication number CN102068997A.
Process characteristic of the present invention is: adopt the series connection of two-stage hydrogenating desulfurization treatment reactor to handle, and the hydrogenating desulfurization treatment reactor adopts the fixed-bed reactor structure.Through sour crudes being carried out double hydrodesulfurization reaction, when guaranteeing hydrogenating desulfurization, can effectively control alkene and reduce, control loss of octane number to reduce sulphur content; Reaction conditions is gentle.The present invention is the Technology that the sour crudes of the more simple environmental protection of a kind of production process reduce sulphur content; This technological operation condition is flexible; Can handle full distillation gasoline or last running gasoline according to the production needs; Light oil products behind the hydro-upgrading needn't alkali cleaning, and the product loss of octane number is little, and yield is greater than 99%.
Compared with prior art, when method provided by the invention was carried out hydrodesulfurization reaction to sour crudes, raw material both can be that catalytic gasoline of whole fraction also can be the last running gasoline after the cutting; The sour crudes sulphur content variation range that this Technology is handled big (150～1200ppm); Raw material need not to carry out pre-treatment before the charging; Reaction conditions is gentle; Product needn't alkali cleaning behind the upgrading; Loss of octane number is little; Technology is simple, and is easy to operate.This technology provides a kind of economy, solution flexibly for producing the gasoline satisfy EUROIII Emission Standard and Europe IV standard.
Description of drawings
Fig. 1 is the process flow diagram of the inventive method.
Embodiment
In conjunction with accompanying drawing method provided by the present invention is carried out detailed explanation.Technical process is described in detail as follows: from the raw material light oil of pipeline 1 after feedstock pump P1 boosts; Through pipeline 2 with get into interchanger E1 after hydrogen from pipeline 13 mixes; With from the material heat exchange of pipeline 6 after after pipeline 3 gets into process furnace H1 heating; Get into one-level hydrodesulphurisatioreactors reactors R1 through pipeline 4, contact with hydrogenating desulfurization processing catalyzer C1 and carry out hydrodesulfurization reaction.One-level hydrodesulphurisatioreactors reactors elute gets into secondary hydrodesulphurisatioreactors reactors R2 through pipeline 5, contacts with Hydrobon catalyst C2 and carries out hydrodesulfurization reaction.Secondary hydrodesulphurisatioreactors reactors elute through pipeline 6 with from the material of pipeline 2 through interchanger E1 heat exchange after pipeline 7 gets into HP separator V1; The elute of reactor drum R2 is after HP separator V1 carries out vapor-liquid separation; The hydrogen rich stream at top gets into thanomin depriving hydrogen sulphide devices to remove in the tail gas behind the hydrogen sulfide through pipeline 8; Mix with fresh hydrogen again after the back gets into circulating hydrogen compressor K1 supercharging from pipeline 10; One the tunnel mixes with gasoline stocks from pipeline 2 via pipeline 11,13, in addition two-way through pipeline 11,12,15 and pipeline 11,12,14 respectively as the cold hydrogen of one-level hydrogenating desulfurization treatment reactor R1, secondary hydrogenating desulfurization treatment reactor R2.The liquid phase elute of HP separator V1 bottom gets into stabilizer tower T1 through pipeline 16, and a stabilizer tower T1 bottoms part is through pipeline 19 withdrawing devices, as the clean gasoline component.Another part gets into tower bottom reboiler E2 through pipeline 17, gets into stabilizer tower T1 again through pipeline 18 again.Stabilizer tower T1 top product gets into return tank V2 through pipeline 20, and through pipeline 23 bleeders, another part gets into overhead condenser E3 through pipeline 21 and gets back to stabilizer tower T1 by pipeline 22 through the isolating dry gas of V2.
The method preparation that catalyzer C1 in the embodiment of the invention provides by the patent of publication number CN102051208A; The method preparation that catalyzer C2 provides by the patent of publication number CN102068997A; And the catalyzer by the preparation of the method for above-mentioned two pieces of publications all is applicable to the present invention.
Following embodiment can make those of ordinary skill in the art more fully understand the present invention, but does not limit the present invention in any way.
Comparative Examples
With a kind of catalytically cracked gasoline is raw oil I, and its feedstock property is as shown in table 1.Catalytic gasoline of whole fraction and conventional Hydrobon catalyst CoMo/Al
2O
3The single hop hydrodesulfurization reaction is carried out in contact, and its reaction conditions and gasoline products character are as shown in table 2.Can find out that from table 2 sulphur content of gasoline products is 35.5 μ g/g, RON loses 6.1 units, and product yield is greater than 99%.
Embodiment 1
With a kind of catalytically cracked gasoline is raw oil II, and its raw oil character is as shown in table 1.Catalytic gasoline of whole fraction contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; One-level hydrodesulphurisatioreactors reactors elute gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction, and the reaction effluent of secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation.
Reaction conditions that one-level hydrodesulphurisatioreactors reactors and secondary hydrodesulphurisatioreactors reactors are concrete and full distillation gasoline character are as shown in table 3, can find out that by table 3 sulphur content of product is 24.3 μ g/g, loss of octane number 0.7, and product yield is greater than 99%.
With a kind of catalytically cracked gasoline is raw oil III, and its feedstock property is as shown in table 1.Catalytic gasoline of whole fraction contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; The material that comes out from the one-level hydrodesulphurisatioreactors reactors gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction; The reaction effluent of secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation; Sulphur content 39.6 μ g/g; Olefin(e) centent 20.5v%, RON only lose 0.3, and product yield is greater than 99%.
With a kind of catalytically cracked gasoline is raw material IV, and its feedstock property is as shown in table 1.Catalytic gasoline of whole fraction contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; The material that comes out from the one-level hydrodesulphurisatioreactors reactors gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction; The reaction effluent of secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation; Sulphur content is 41.9 μ g/g; Olefin(e) centent is 21.3v%, RON loss 2.7, and product yield is greater than 99%.
Embodiment 4
With a kind of catalytically cracked gasoline is raw material V, and its feedstock property is as shown in table 1.Catalytic gasoline of whole fraction contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; The material that comes out from the one-level hydrodesulphurisatioreactors reactors gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction; The reaction effluent of secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation; Sulphur content is 89.8 μ g/g; Olefin(e) centent is 25.9v%, the RON free of losses, and product yield is greater than 99%.
Embodiment 5
With a kind of catalytically cracked gasoline is raw material VI, and its feedstock property is as shown in table 1.Catalytic gasoline of whole fraction contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; The material that comes out from the one-level hydrodesulphurisatioreactors reactors gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction; The reaction effluent of secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation; Sulphur content is 90.4 μ g/g; Olefin(e) centent is 29.6v%, RON loss 1.3, and product yield is greater than 99%.
Embodiment 6
With a kind of catalytically cracked gasoline is raw material VII, and its feedstock property is as shown in table 1.Catalytically cracked gasoline contacts with Hydrobon catalyst C1 in the one-level hydrodesulphurisatioreactors reactors and carries out the selective hydrodesulfurization reaction; The material that comes out from the one-level hydrodesulphurisatioreactors reactors gets into the secondary hydrodesulphurisatioreactors reactors again and Hydrobon catalyst C2 carries out the deep hydrodesulfurizationof reaction; The reaction effluent of a secondary hydrogenating desulfurization treatment reactor gets into the product jar and obtains gasoline products after cooling, separation; Sulphur content is 94.8 μ g/g; Olefin(e) centent is 15.6v%, the RON free of losses, and product yield is greater than 99%.
Table 1.
Table 2.
| Comparative Examples | |
| Raw oil | Raw material I |
| Catalyzer | CoMo/γ-Al 2O 3 |
| Reaction conditions | |
| Temperature of reaction, ℃ | 260 |
| Hydrogen pressure, MPa | 1.1 |
| Hydrogen to oil volume ratio, ml/ml | 300 |
| Volume space velocity, h -1 | 2.0 |
| Product property | |
| Density (20 ℃), g/cm 3 | 0.72 |
| S，μg/g | 35.5 |
| Olefin(e) centent, volume % | 24.9 |
| Desulfurization degree, m% | 81.4 |
| The alkene saturation exponent, v% | 34.5 |
| RON | 85.1 |
| The RON loss | 6.1 |
| Product yield, m% | ＞99％ |
Table 3.
(desulfurization degree: HDS%=(S
Raw material-S
Product)/S
Raw material* 100; Alkene saturation exponent: HYD%=(O
Raw material-O
Product)/O
Raw material* 100)
Claims (10)
1. method that reduces the sour crudes sulphur content may further comprise the steps:
1. the light oil raw material gets into one-level hydrogenating desulfurization treatment reactor, with Hydrobon catalyst C1 contact reacts;
2. the elute that 1. reacts of step gets into the secondary hydrodesulphurisatioreactors reactors, with Hydrobon catalyst C2 contact reacts;
3. the elute that 2. reacts of step obtains the light oil products of low sulfur content after gas-liquid separation;
Said one-level hydrogenating desulfurization treatment reactor and secondary hydrogenating desulfurization treatment reactor all adopt the fixed-bed reactor structure;
Said Hydrobon catalyst C1 is group vib base metal and the group VIII non-precious metal catalyst that loads on the complex carrier.
The carrier of said Hydrobon catalyst C2 is one or more the composite oxides in aluminum oxide, zirconium white, the titanium oxide, and active ingredient is nickel and/or cobalt.
2. method according to claim 1; It is characterized in that: the hydrogen rich gas that 3. step obtains after the gas-liquid separation removes hydrogen sulfide; And with after fresh hydrogen is mixed; The a part of mixing with raw oil carried out hydrodesulfurization reaction, and another part is as the cold hydrogen of one-level hydrogenating desulfurization treatment reactor and secondary hydrogenating desulfurization treatment reactor.
3. method according to claim 1 is characterized in that: the liquid efflunent that 3. step obtains after the gas-liquid separation is handled top, back elute entering return tank through stabilizer tower and is isolated dry gas, and remaining liquid is back to stabilizer tower through overhead condenser.
4. method according to claim 1; It is characterized in that: the liquid efflunent that 3. step obtains after the gas-liquid separation is circulated to stabilizer tower handle the part entering tower bottom reboiler of bottom, back elute through stabilizer tower after, and another part is the light oil products of low sulfur content.
5. method according to claim 1 is characterized in that: the reaction conditions of said one-level hydrogenating desulfurization treatment reactor: hydrogen partial pressure 1.0～3.0MPa, 250～350 ℃ of temperature of reaction, volume space velocity 1.0～4.0h
-1, hydrogen to oil volume ratio 200～700ml/ml.
6. method according to claim 1 is characterized in that: the reaction conditions of said secondary hydrogenating desulfurization treatment reactor: hydrogen partial pressure 1.0～3.0MPa, 250～380 ℃ of temperature of reaction, volume space velocity 2.0～6.0h
-1, hydrogen to oil volume ratio 200～700ml/ml.
7. method according to claim 1 is characterized in that: the complex carrier of said Hydrobon catalyst C1 is the complex carrier of aluminum oxide and molecular sieve, perhaps is the complex carrier of amorphous silicon aluminium and molecular sieve.
8. according to claim 1 or 7 described methods, it is characterized in that: said complex carrier is the complex carrier of aluminum oxide and ZSM-5; Said group vib base metal is molybdenum and/or tungsten, is benchmark with complex carrier weight, and the content of described molybdenum and/or tungsten is 5.0～15.0%; Said group VIII base metal is nickel and/or cobalt, is benchmark with the vehicle weight, and the content of nickel and/or cobalt is 0.5～6.0%.
9. method according to claim 1 is characterized in that: be benchmark with the vehicle weight, the content of nickel and/or cobalt is 1.0～20.0% among the said Hydrobon catalyst C2.
10. method according to claim 1; It is characterized in that: method according to claim 1 is characterized in that: said light oil raw material is one or more in catalytically cracked gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, steam cracking gasoline, the pyrolysis gasoline.
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| CN104650975A (en) * | 2013-11-22 | 2015-05-27 | 中国石油天然气股份有限公司 | Deep desulfurization method of gasoline |
| CN104650975B (en) * | 2013-11-22 | 2016-09-07 | 中国石油天然气股份有限公司 | A kind of method of deep desulfurization of gasoline |
| CN108611119A (en) * | 2016-12-12 | 2018-10-02 | 河北新启元能源技术开发股份有限公司 | Naphtha catalytic reforming unit and its catalytic reforming process |
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Application publication date: 20120404 |